WO2005120681A1 - Processus d'adsorption par variation de la pression de recyclage complet a deux etages en vue de separer des gaz - Google Patents

Processus d'adsorption par variation de la pression de recyclage complet a deux etages en vue de separer des gaz Download PDF

Info

Publication number
WO2005120681A1
WO2005120681A1 PCT/CN2005/000641 CN2005000641W WO2005120681A1 WO 2005120681 A1 WO2005120681 A1 WO 2005120681A1 CN 2005000641 W CN2005000641 W CN 2005000641W WO 2005120681 A1 WO2005120681 A1 WO 2005120681A1
Authority
WO
WIPO (PCT)
Prior art keywords
adsorption
stage
pressure swing
gas
swing adsorption
Prior art date
Application number
PCT/CN2005/000641
Other languages
English (en)
Chinese (zh)
Inventor
Yuwen Song
Original Assignee
Chengdu Tianli Chemical Engineering Technology Co., Ltd.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Chengdu Tianli Chemical Engineering Technology Co., Ltd. filed Critical Chengdu Tianli Chemical Engineering Technology Co., Ltd.
Priority to US11/570,312 priority Critical patent/US8545601B2/en
Priority to DE602005026125T priority patent/DE602005026125D1/de
Priority to EA200700011A priority patent/EA012820B1/ru
Priority to EP05745102A priority patent/EP1772182B1/fr
Priority to AT05745102T priority patent/ATE496676T1/de
Priority to PL05745102T priority patent/PL1772182T3/pl
Priority to AU2005251848A priority patent/AU2005251848B2/en
Priority to JP2007526170A priority patent/JP4579983B2/ja
Publication of WO2005120681A1 publication Critical patent/WO2005120681A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/104—Alumina
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40001—Methods relating to additional, e.g. intermediate, treatment of process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40013—Pressurization
    • B01D2259/40015—Pressurization with two sub-steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40035—Equalization
    • B01D2259/40041—Equalization with more than three sub-steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
    • B01D2259/40075—More than ten
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/406—Further details for adsorption processes and devices using more than four beds
    • B01D2259/4065—Further details for adsorption processes and devices using more than four beds using eight beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/406—Further details for adsorption processes and devices using more than four beds
    • B01D2259/4068—Further details for adsorption processes and devices using more than four beds using more than ten beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/414—Further details for adsorption processes and devices using different types of adsorbents
    • B01D2259/4141—Further details for adsorption processes and devices using different types of adsorbents within a single bed
    • B01D2259/4145—Further details for adsorption processes and devices using different types of adsorbents within a single bed arranged in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B01D53/053—Pressure swing adsorption with storage or buffer vessel

Definitions

  • the invention relates to a two-stage full recovery pressure swing adsorption gas separation method, which uses a two-stage pressure swing adsorption gas separation technology, and belongs to the field of pressure swing adsorption gas separation. Background technique
  • the present invention is an improvement of the above-mentioned pressure swing adsorption gas separation technology, with almost no loss of effective gas, and under appropriate adsorption pressure, There is no need to use a complicated process of vacuuming, which not only saves investment, but also does not have power consumption of power equipment. Disclosure of invention
  • the invention is used for separating the easily adsorbed phase and the difficult-adsorbing phase component from the mixed gas, and the product may be an easy-adsorbing phase component or a difficult-adsorbing phase component, and may also be an easily adsorbable phase and a difficult-adsorbing phase component.
  • the easily adsorbed phase and the poorly adsorbed phase are relative rather than absolute, and the same component is an easily adsorbable phase component in a mixed gas, but may be difficult to adsorb in another mixed gas.
  • the phase component even if the same component is in the same mixed gas, may be an easy-adsorbing phase component or a difficult-adsorbing phase component due to the different purposes to be achieved.
  • the fractional and difficult to adsorb phase components may be a single component or a sum of several components.
  • the ammonia conversion gas there are components such as hydrogen sulfide, organic sulfur, gaseous water, carbon dioxide, methane, carbon monoxide, nitrogen, oxygen, argon, and hydrogen.
  • hydrogen sulfide, organic sulfur When the gas is used to produce urea, hydrogen sulfide, organic sulfur,
  • the four components, such as gaseous water, and carbon dioxide, are called easy-adsorbed phases.
  • the six components of formazan, carbon monoxide, nitrogen, oxygen, argon, and hydrogen are called refractory phase components; they are used to produce 99.9%.
  • the product is hydrogen
  • nine components such as hydrogen sulfide, organic sulfur, gaseous water, carbon dioxide, methane, carbon monoxide, nitrogen, oxygen and argon are called components of the easily adsorbable phase
  • hydrogen is called the component of the difficult phase.
  • the nitrogen in the ammonia conversion gas is used to produce urea, and nitrogen is a component that is difficult to adsorb; when used to produce 99.9% of the product hydrogen, nitrogen is an easily adsorbable phase component, formazan, Carbon monoxide and oxygen are the same as nitrogen.
  • the object of the present invention is to provide a two-stage full recovery pressure swing adsorption gas separation method with economical investment and low operating cost, which uses different equipment and adsorbent combinations to solve the above problems in the prior art. It has the advantage of greatly saving operating costs compared with the prior art, and minimizes - Less effective gas loss from the device.
  • the object of the invention is to implement as follows:
  • the invention adopts a two-stage full recovery pressure swing adsorption gas separation method, which is used for separating the easily adsorbed phase and the difficult-adsorbing phase component from the mixed gas, and the product may be an easy-adsorbing phase component or a difficult-adsorbing phase component. It can also be an easy-adsorbing phase and a difficult-adsorbing phase component.
  • This method uses a two-stage pressure swing adsorption device to operate in series. The mixed gas first enters the first stage pressure swing adsorption gas separation device, and the easily adsorbed phase components in the mixed gas.
  • the intermediate mixture obtained from the outlet of the adsorption tower of the first stage of the pressure swing adsorption gas separation device enters the second stage pressure swing adsorption gas separation device, and the easy adsorption phase component in the intermediate mixture gas is introduced into The one-step adsorption, the unadsorbed difficult-adsorbed phase component enters the next stage as a product, and the second-stage pressure swing adsorption gas separation device returns to the first stage except for the difficult-adsorption phase component of the next stage.
  • the pressure swing adsorption gas separation device pressurizes the adsorption tower, and the adsorption tower of the first stage pressure swing adsorption gas separation device sequentially undergoes adsorption in one cycle, and ends Pressure depressurization 2ED', reverse buck BD, two-stage gas boost 2ER, two-stage equalization boost 2ER', final boost FR process step, second stage pressure swing adsorption gas separation device adsorption tower in one cycle
  • the process steps of adsorption 4, forward equalization step-down ED, reverse BD, reverse equalization step-up ER, and final step-up FR are sequentially performed.
  • the adsorption tower of the pressure swing adsorption gas separation device increases the forward pressure equalization step ED step after the adsorption A step, and increases the reverse pressure equalization step ER step after the pressure equalization step 2ER' step.
  • the first stage of the pressure swing adsorption gas separation unit adsorption tower increases the vacuum after the reverse pressure reduction BD step VC or (and) the second stage pressure swing adsorption gas separation unit adsorption tower increases the vacuum VC after the reverse pressure reduction BD step.
  • the second stage of the pressure swing adsorption gas separation device adsorption tower increases the downstream PP step after the forward pressure equalization step ED step, and increases the cleaning P after the second stage pressure swing adsorption gas separation unit adsorption tower process cycle step reverses the BD step.
  • the gas for cleaning the P step is directly from the adsorption tower which is in the step of discharging PP or the buffer tank V from which the gas of the step PP is stored in the storage adsorption tower.
  • the second stage of the pressure swing adsorption gas separation device adsorption tower increases the step of the PP step 1 and the step of discharging the PP2 after the step of the forward pressure equalization step ED, and the adsorption tower of the second stage of the pressure swing adsorption gas separation unit is after the step of the reverse BD
  • the gas in the adsorption tower cleaning step P1 is directly from the adsorption tower which is in the step of discharging PP2 or the buffer tank VI from the step of storing the adsorption step to the PP2 step, and the adsorption tower is cleaned in the P2 step.
  • the gas is directly from the adsorption column that is in the process of the PP1 step or the buffer tank V2 from which the gas in the PP1 step is stored.
  • the second stage of the pressure swing adsorption gas separation device adsorption tower increases the step of the PP step 1 , the step of discharging the PP 2 and the step of discharging the PP 3 after the step of the forward pressure equalization step ED, and the adsorption tower of the second stage pressure swing adsorption gas separation device is After the BD step is reversed, the cleaning P1 step, the cleaning P2 step, and the cleaning P3 step are added.
  • the gas in the adsorption tower cleaning step P1 is directly from the adsorption tower that is in the step of discharging PP3 or the buffer tank from the step of storing the adsorption step in the PP3 step.
  • the gas in the adsorption tower cleaning P2 step comes directly from the positive
  • the adsorption tower in the step of discharging PP2 or the buffer tank V4 from the step of storing the adsorption step of the PP2 step, the gas in the adsorption tower cleaning step P3 is directly from the adsorption tower which is in the step of discharging PP1 or from the storage adsorption tower.
  • Buffer tank V5 for PP1 step gas is directly from the adsorption tower which is in the step of discharging PP1 or from the storage adsorption tower.
  • the average concentration of the components of the easily adsorbable phase is greater than 30% in the mixture of the top 5 of the adsorption tower.
  • the average concentration of the easily adsorbable phase components in the mixture discharged at the top of the adsorption tower is greater than 75%.
  • the average concentration of the components of the easily adsorbed phase in the outlet gas of the first stage of the pressure swing adsorption device is greater than or equal to 2V%.
  • the second stage of the pressure swing adsorption gas separation unit adsorption tower performs the reverse BD step, first placed in the buffer tank V6, and then placed in the buffer tank V7.
  • the pressure equalizing gas below 50% enters the adsorption tower for the pressure equalization from the bottom of the adsorption tower.
  • the invention is used for separating the easily adsorbed phase and the difficult-adsorbing phase component from the mixed gas, and the product may be an easy-adsorbing phase component or a difficult-adsorbing phase component, and may also be an easily adsorbable phase and a difficult-adsorbing phase component.
  • the method uses a two-stage pressure swing adsorption device to operate in series, and the mixed gas first enters the first stage pressure swing adsorption gas separation device, and the components of the easily adsorbed phase in the mixed gas are adsorbed and concentrated into products, from the first Section of the pressure swing adsorption gas 20 separation unit
  • the intermediate mixture obtained at the outlet of the adsorption tower enters the second stage pressure swing adsorption gas separation device, and further adsorbs the easily adsorbed phase components in the intermediate mixture, and the unadsorbed difficult adsorption phase group
  • the product enters the next stage as a product, and the first stage of the pressure swing adsorption gas separation device reverses the pressure drop.
  • the gas of the BD1 step returns to the first stage of the pressure swing adsorption gas separation device to boost the adsorption tower from the bottom, and the second stage pressure swing adsorption The gas separation device returns to the first stage change except for the difficult-adsorbed phase components of the next stage.
  • the pressure-adsorption gas separation device boosts the adsorption tower.
  • the adsorption tower of the first-stage pressure swing adsorption gas separation device undergoes adsorption A, forward pressure equalization and pressure reduction ED, reverse pressure reduction BD1, and reverse down in a cycle.
  • the first stage of the pressure swing adsorption gas separation unit adsorption tower increases the vacuum VC after the reverse pressure reduction two BD2 step or (and) the second stage pressure swing adsorption gas separation unit adsorption tower increases the vacuum VC after the reverse step BD step ;
  • the second stage of the pressure swing adsorption gas separation device adsorption tower increases the step of the PP1 step, the step of displacing the PP2, and the step of displacing the PP3 after the step of the forward pressure equalization step ED, and the second stage of the pressure swing adsorption gas separation device After the reverse BD step, the cleaning P1 step, the cleaning P2 step, and the cleaning P3 step are added.
  • the gas in the adsorption tower cleaning PI step is directly from the adsorption tower which is in the step of discharging PP3 or the buffer tank V3 from the step of storing the PP3 step in the storage adsorption tower, and the gas in the adsorption tower cleaning step P2 is directly from the step of being in the step of discharging PP2.
  • the average concentration of the easily adsorbable phase components in the mixture discharged at the top of the adsorption tower is greater than 40°/. .
  • the average concentration of the easily adsorbable phase components in the mixture discharged at the top of the adsorption tower is greater than 75%.
  • the average concentration of the components of the easily adsorbed phase in the outlet gas of the first stage of the pressure swing adsorption device is greater than or equal to 2%V.
  • the pressure of the raw material mixture is greater than or equal to 1. 8 MPaG.
  • the average concentration of the easily adsorbable phase components in the finally released mixture is greater than 30%.
  • the average concentration of the easily adsorbable phase components in the finally released mixture is greater than 80%.
  • the adsorption tower is filled with activated alumina and fine pore silica gel, the active alumina is packed at the bottom of the adsorption tower, and the fine pore silica gel is packed in the upper part of the adsorption tower.
  • the second stage of the pressure swing adsorption gas separation device is only filled with fine pore silica gel in the adsorption tower.
  • the adsorbent of the first stage of the pressure swing adsorption gas separation device in the adsorption tower from bottom to top is activated alumina and fine pore silica gel or activated alumina and activated carbon or activated alumina, activated carbon and molecular sieve; the second stage pressure swing adsorption In the gas separation device, the adsorbent packed in the adsorption tower is activated carbon and molecular sieve or molecular sieve.
  • the adsorbent in the adsorption tower of the first stage of the pressure swing adsorption gas separation device is activated alumina and molecular sieve in order from the bottom to the top; the adsorbent loaded in the adsorption tower of the second stage pressure swing adsorption gas separation device is a molecular sieve.
  • the adsorbent in the adsorption tower of the first stage of the pressure swing adsorption gas separation device is activated alumina and molecular sieve in order from the bottom to the top; the adsorbent loaded in the adsorption tower of the second stage pressure swing adsorption gas separation device is a molecular sieve.
  • the invention can maximize the recovery rate of the effective gas to 99.9%, and reduce the power consumption by 50 to 90% (increased with the increase of the adsorption pressure). It can be said that the present invention is an existing gas separation method ( Revolutionary changes including wet gas separation technology and pressure swing adsorption gas separation technology have completely solved the problem of effective gas loss and high power consumption of the device.
  • BRIEF DESCRIPTION OF THE DRAWINGS BRIEF DESCRIPTION OF THE DRAWINGS
  • Fig. 1 is a flow chart showing the operation steps of a process step of an adsorption tower of a first stage pressure swing adsorption apparatus according to Embodiment 1 of the present invention.
  • Fig. 2 is a flow chart showing the operation steps of the adsorption step of the second stage pressure swing adsorption device of the first embodiment of the present invention.
  • Figure 3 is a process flow diagram of Embodiment 1 of the present invention. The best way to implement the invention
  • the mixed gas of the invention may be synthetic ammonia conversion gas, synthetic ammonia gas, synthesis gas, water gas, natural gas, semi-water gas, blast furnace gas, gas gas, cracked dry gas, oil field associated gas and oil gas, etc., or any other mixed composition.
  • the invention adopts a two-stage full recovery pressure swing adsorption gas separation method, which is used for separating the easily adsorbed phase and the difficult-adsorbing phase component from the mixed gas, and the product may be an easy-adsorbing phase component or a difficult-adsorbing phase component. It can also be an easy-adsorbing phase and a difficult-adsorbing phase component.
  • This method uses a two-stage pressure swing adsorption device to operate in series. The mixed gas first enters the first stage pressure swing adsorption gas separation device, and the easily adsorbed phase components in the mixed gas.
  • the intermediate mixture obtained from the outlet of the adsorption tower of the first stage of the pressure swing adsorption gas separation device enters the second stage pressure swing adsorption gas separation device, and further extracts the easily adsorbed phase components in the intermediate mixture.
  • Adsorbed, the unadsorbed refractory phase component enters the next stage as a product.
  • the second stage of the pressure swing adsorption gas separation unit returns to the first stage of the pressure change except for the difficult phase of the next stage.
  • the adsorption gas separation device boosts the adsorption tower, and the average concentration of the components of the easily adsorbed phase in the outlet gas of the adsorption tower of the first stage pressure swing adsorption device is generally greater than or equal to 2% (V), the second stage pressure swing adsorption device is used to remove the easily adsorbed phase components in the outlet gas of the first stage pressure swing adsorption device to the level required by the next stage, and each of the two stages of pressure swing adsorption devices
  • the adsorption towers are sequentially subjected to the following steps in one cycle.
  • the first stage pressure swing adsorption device The first stage pressure swing adsorption device:
  • the mixed gas is sent to the adsorption tower inlet of the adsorption step, the adsorbent in the adsorption tower adsorbs a part of the easily adsorbable phase component in the mixed gas, the unadsorbed difficult adsorbed phase component and a part of the easily adsorbable phase component are exported.
  • the end flows out into the adsorption tower of the second stage pressure swing adsorption device in the adsorption step.
  • the total amount of the adsorbent phase adsorbed by the adsorbent increases continuously, and when the adsorbent adsorbs the above components, the adsorption stops. At this point, the adsorption ends.
  • the concentration of the hard-to-adsorbed phase components in the dead space gas in the adsorption tower is relatively high, and this part of the difficult-to-absorb phase components needs to be recycled.
  • the dead space gas is discharged from the outlet of the adsorption tower into the corresponding adsorption tower of the completed evacuation step in this section.
  • the pressure of each gas is equalized once.
  • the concentration of the components is constantly increasing.
  • the number of pressure equalization is determined by the adsorption pressure and the concentration of the easily adsorbable phase at the outlet of the adsorption tower after the end of adsorption. Under normal circumstances, the concentration of the easily adsorbable phase at the top of the adsorption tower should be greater than the end of the final forward pressure equalization ED. 30V%, preferably greater than 75V%.
  • the dead space gas is discharged from both ends of the adsorption tower into the corresponding adsorption tower of the completed regeneration step of this section, and the gas is uniformly pressurized once per row.
  • the outlets at both ends of the adsorption tower The concentration of the easily adsorbable phase components is continuously increased, and at the same time, the phase components which are difficult to adsorb are recycled.
  • the upper and lower ends of the adsorption tower can be simultaneously carried out, or the pressure can be gradually reduced from the top of the adsorption tower first, and simultaneously adsorbed to the same adsorption in the late stage before the forward pressure equalization and pressure reduction balance.
  • the tower performs reverse pressure equalization and depressurization, the purpose is to increase the concentration of the easily adsorbable phase components in the adsorption tower and recover the components of the difficult adsorption phase. It is also possible to carry out the forward pressure equalization and pressure reduction first, and stop the forward pressure equalization before the pressure of the two towers is balanced. The pressure is reduced, and then the reverse pressure equalization is performed. The former case can improve the utilization rate of the adsorbent.
  • the gas released from the bottom should be less than the gas released from the top.
  • the step of equalizing and lowering the pressure at both ends of the adsorption tower of the present invention is different from the step of depressing and lowering the pressure of the conventional adsorption tower.
  • the normal adsorption tower pressure equalization step ED step gas is released from the outlet end of the adsorption tower, that is, the present According to the invention, the forward pressure equalization is reduced, and the pressure equalization and pressure reduction at both ends of the adsorption tower of the present invention is released from the both ends of the inlet and outlet of the adsorption tower.
  • the first several equalization pressures may also adopt the forward pressure equalization step-down ED, and the subsequent several equalization pressures or the last equalization pressure adopts the two-stage equalization pressure reduction 2ED ', after the pressure equalization and pressure reduction is completed.
  • the concentration of the easily adsorbable phase components of the product can still meet the production requirements.
  • the number of pressure equalization is determined by the adsorption pressure and the concentration of the easily adsorbable phase at the outlet of the adsorption tower after the end of adsorption.
  • the concentration of the easily adsorbable phase at the top of the adsorption tower should be More than 30V%, preferably more than 75V%; the concentration of the readily adsorbable phase component at the bottom of the adsorption tower should be greater than 30V%, preferably greater than 80V%.
  • the components of the easily adsorbed phase in the adsorption tower are sent to the next stage until the pressure of the next stage is balanced, and the components are easily adsorbed or used as a product, or as a fuel. Can also be emptied.
  • the difficult-adsorbed phase at the bottom of the adsorption tower is discharged into the buffer tank for storage, and the gas in the buffer tank is used to pressurize the adsorption tower from the bottom of the adsorption tower. Under normal circumstances, the reverse pressure is reduced.
  • the concentration of the readily adsorbable phase component at the bottom of the adsorption column should be greater than 30V%, preferably greater than 80V%. .
  • the components of the adsorption phase in the adsorption tower are sent to the next stage until the pressure of the next stage is balanced, and the components of the phase are easily adsorbed or used as a product, or as a fuel.
  • Vacuuming VC After the reverse buck BD is finished, the components of the easily adsorbed phase adsorbed by the adsorbent are pumped out from the bottom of the adsorption tower by a vacuum pump and sent to the next stage.
  • the purge CP step may be employed, and the gas used for purging is a dry adsorbent phase component product or other dry gas in the system. Use this step when you need to reduce the amount of adsorbent.
  • the gas released by the adsorption tower reverse pressure-reducing BD1 step of the first stage of the pressure swing adsorption gas separation device is returned to the outlet end of the adsorption tower of the first stage of the pressure swing adsorption gas separation device.
  • the buck of the buck 'BD or vacuum pump step is boosted. Increasing this step increases the effective gas recovery of the unit.
  • the second stage of the pressure swing adsorption gas separation device After the reverse buck BD or vacuum VC or a gas boost 2ER1 is completed, the second stage of the pressure swing adsorption gas separation device returns to the first stage of the pressure swing adsorption gas except for the difficult adsorption phase component of the next stage.
  • the separation end of the separation column of the separation device pressurizes the adsorption column that has completed the reverse pressure reduction BD or the vacuum VC step. Increasing this step increases the effective gas recovery of the unit.
  • the gas discharged from the two stages of pressure equalization and pressure reduction 2ED' is used to enter the adsorption tower from the inlet and outlet, so that the adsorption tower gradually increases the pressure, and the pressure equalization at both ends is 2ER'
  • the number of equalization steps 2ED ' at both ends is equal.
  • the step of pressure equalization 2ER' at both ends of the adsorption tower is different from the normal pressure equalization step ER step.
  • the normal adsorption tower pressure equalization step ER step gas enters from the outlet end of the adsorption tower, and this section adsorbs The pressure equalization of the two ends of the tower 2ER' step gas is entered from the inlet and outlet of the adsorption tower.
  • the pressure equalization step-up ER step gas of the adsorption tower enters from the outlet end of the adsorption tower and does not enter from the inlet end.
  • the gas discharged from the forward pressure equalizing step is used to enter the adsorption tower which has completed the reverse BD or vacuum C or the cleaning P step from the outlet end.
  • the adsorption tower is gradually increased in pressure, and the equalization pressure is equal to the number of times of pressure equalization. Each time the pressure-boosted gas comes from the pressure equalizing gas of different adsorption towers
  • the adsorption tower is pressurized from the top end by the adsorption tower outlet gas in the adsorption step until it reaches the adsorption pressure.
  • the adsorption tower outlet gas of the first stage pressure swing adsorption device in the adsorption step is sent to the adsorption tower of the second stage pressure swing adsorption device in the adsorption step, and the adsorbent in the adsorption tower selectively adsorbs the easy adsorption phase group Divided from the exit end into the next section.
  • the total amount of easily adsorbed phase components adsorbed by the adsorbent increases continuously.
  • the adsorbent adsorbs the easily adsorbed phase components, the intake is stopped. At this time, the adsorption ends, and the concentration of the easily adsorbed phase components in the outlet gas is increased. Controlled according to production needs, up to a few ppm.
  • the concentration of the components in the dead space gas in the adsorption tower is relatively high, and this part of the difficult-to-absorb phase components needs to be recycled.
  • the dead space gas is discharged from the outlet of the adsorption tower into the corresponding adsorption tower of the completed evacuation step in this section.
  • the pressure of each gas is equalized once. As the number of equalization times increases, the easily adsorbed phase at the outlet of the adsorption tower
  • the concentration of the components is constantly increasing.
  • the number of pressure equalizations is determined by the adsorption pressure and the concentration of the readily adsorbable phase components at the outlet of the adsorption tower after the end of adsorption.
  • the gas in the adsorption tower is directly placed in another adsorption tower to clean the adsorbent component adsorbed on the adsorbent, or it can be smoothly discharged into the buffer tank, and then buffered.
  • the gas in the tank is placed in another adsorption tower to clean the adsorbable phase components adsorbed on the adsorbent, so that the adsorbent can be regenerated.
  • the PP can be divided into two times, or it can be divided into two or three times, or even many times. The more times the PP is discharged, the better the cleaning effect, the less the amount of adsorbent, but the non-standard equipment, the special program control valve, and the oil pressure.
  • the adsorption-adsorbed phase component and other components adsorbed by the adsorbent are pumped out from the bottom of the adsorption tower into the first stage of the pressure swing adsorption gas separation device to regenerate the adsorbent;
  • the mixed gas adsorbed on the adsorbent is washed by the mixed gas in the PP step, and the mixed gas after the adsorbent is regenerated and washed is placed in the adsorption tower of the first stage pressure swing adsorption gas separation device.
  • the gas discharged from the forward pressure equalization step is used to enter the adsorption tower that has completed the reverse BD or vacuum C or the cleaning P step from the outlet end, so that the adsorption tower is gradually ⁇ raises the pressure, and the equalization pressure boost is equal to the equalization pressure reduction.
  • Each pressure equalization pressure is derived from the pressure equalization gas of different adsorption towers.
  • the adsorption tower is pressurized from the top end by the adsorption tower outlet gas in the adsorption step until it rises to the adsorption pressure.
  • the raw material gas in this example is an ammonia conversion gas, including synthetic ammonia conversion gas using coal, natural gas, oil and others as raw materials.
  • a total of 11 adsorption towers A to K constitute the first stage pressure swing adsorption device, and the adsorbent in the adsorption tower from bottom to top is activated alumina and Fine pore silica gel, running single tower adsorption 9 times pressure equalization program; 8 towers of adsorption tower a ⁇ h form the second stage pressure swing adsorption device, the adsorbent packed in the adsorption tower is fine pore silica gel, and the single tower adsorption is performed six times. Pressure program.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea, and the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower of the second stage of the pressure swing adsorption device is less than 0.2% (V) to meet the needs of the next step of ammonia synthesis.
  • the shift gas enters the adsorption tower of the first stage pressure swing adsorption device in the adsorption step, and the adsorbent in the adsorption tower selectively adsorbs the water, organic sulfur, inorganic sulfur and carbon dioxide components in the shift gas, and the unadsorbed part of the carbon dioxide
  • the non-adsorbable carbon monoxide, formazan, nitrogen, hydrogen and other components are discharged from the outlet end into the second stage of the pressure swing adsorption device in the adsorption step, the adsorbent in the adsorption tower selectively adsorbs carbon dioxide, which is not easily adsorbed.
  • Components such as carbon monoxide, methane, nitrogen, hydrogen, etc.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • the two ends are reduced by 2E5D', the two ends are reduced by 2E6D', the two ends are reduced by 2E7D', the two ends are reduced by 2E8D', the two ends are reduced by 2E9D', the product carbon dioxide reverse buck BD, two Section gas boost 2ER, 9E rise at both ends 2E9R', 8E rise at both ends 2E8R', 7E rise at both ends 2E7R', 6E rise at both ends 2E6R', 5E rise at both ends 2E5R', both ends 2E4fT, 2E3R' at both ends, 2E2R' at both ends, 2E1R' at both ends, final step-up FR pressure swing adsorption process step, the first stage pressure swing adsorption device in product carbon dioxide pressure reduction
  • the gas obtained in the BD step is the carbon dioxide of the product.
  • the adsorption tower of the second stage pressure swing adsorption device undergoes adsorption A in one cycle, E1 D, E2D, E3D, E4D, E4D. , five average E5D, six average E6D, reverse BD1, reverse BD2, six average E6R, five average E5R, four average E4R, three average E3R, two E2R, one equal E1 R, final boost FR pressure swing adsorption process step
  • the second stage pressure swing adsorption device is in the adsorption step of the adsorption tower outlet to discharge the mixture mainly nitrogen, hydrogen products, which also contain a small amount of carbon monoxide And methane.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step.
  • the gas in the step is all returned to the first stage of the pressure swing adsorption device.
  • the carbon adsorption tower BD adsorption tower is boosted, referred to as the second stage gas boost 2ER.
  • the A tower has completed the final boost FR step, opening the program control valve 1A, 2A, changing the gas through the pipeline
  • G11 enters adsorption tower A.
  • the adsorbent selectively adsorbs water, organic sulfur, inorganic sulfur and carbon dioxide components in the shift gas, unabsorbed part of carbon dioxide and non-adsorbable carbon monoxide, formazan, Nitrogen, hydrogen and other components flow out from the outlet end through the programmed valve 2A into the adsorption tower of the second stage of the pressure swing adsorption device in the adsorption step.
  • the adsorbent adsorbs water, organic sulfur and inorganic sulfur and carbon dioxide. The total amount of the fraction is continuously increased.
  • the program-controlled valves 1A and 2k are closed, and the carbon dioxide concentration in the outlet gas is controlled at 6 to 15 ° /. (V).
  • the program-controlled valves 3A, 3C, 11A and 11C are opened, and the gas in the A tower enters the C-column through the pipes G13 and Gi ll, and the C-column is pressure-boosted at both ends (referred to as 2E1 R'), when A and After the C tower pressure is basically balanced, the program control valves 3A, l lCo are closed.
  • the program-controlled valves 4A, 4D and 11D are opened, and the gas in the A tower enters the D tower through the pipelines G14 and G11, and the two towers are subjected to the second equalizing step-up (referred to as 2E2R').
  • the control gates 4D, 11A and 11D are closed.
  • the program-controlled valves 4E, 12A and 12E are opened, and the gas in the A tower enters the E tower through the pipes G14 and G112, and the E-column is subjected to three equalizing pressure boosting at both ends (referred to as 2E3R'). After the A and E tower pressures are substantially balanced, the program-controlled valves 4A, 4E and 12E are closed.
  • the program-controlled valves 5A, 5F and 12F are opened, and the gas in the A tower enters the F tower through the pipes G15 and G112, and the F-column is subjected to four equalizing pressure boosting at both ends (referred to as 2E4R').
  • the program control valves 5F, 12A and 12F are closed.
  • the program-controlled valves 5G, 13A and 13G are opened, and the gas in the A tower enters the G tower through the pipelines G15 and G113, and the G tower is subjected to five equalizing pressure boosting at both ends (referred to as 2E5R').
  • the program-controlled valves 5A, 5G and 13G are closed.
  • the program-controlled valves 61, 8A and 81 are opened, and the gas in the A tower enters the I tower through the pipelines G16 and G18, and the seven towers are pressure-boosted at both ends (abbreviated as 2E7R').
  • the program-controlled valves 6A, 61 and 81 are closed.
  • the program-controlled valves 7A, 7J and 8J are opened, and the gas in the A tower enters the J tower through the pipes G17 and G18, and the eight-stage equalizing pressure boosting (referred to as 2E8R') is performed on the J tower.
  • the program control valves 7J, 8A and 8J are closed.
  • G17 and G19 enter the K tower and the K tower is subjected to nine equal pressure boosting at both ends (referred to as 2E9R ').
  • the program-controlled valves 7A, 7K and 9K are closed.
  • the concentration of the easily adsorbable phase at the top of the adsorption tower is greater than 70V%; the concentration of the easily adsorbable phase at the bottom of the adsorption tower is greater than 75V%.
  • the program control valve KV-14a is opened first, and the product carbon dioxide in the A tower is depressurized into the product carbon dioxide intermediate buffer tank V9.
  • the program control valve KV14a is closed. Then, open the KV14 of the control cabinet, and reduce the carbon dioxide of the product in the A tower into the carbon dioxide buffer tank V8.
  • the pressure of the A tower is close to the pressure of V8, close the program control valve KV-14.
  • the program control ⁇ 10A is opened, the gas in the buffer tanks V6 and V7 enters the A tower to boost the A tower, and when the pressures of the buffer tanks V6 and V7 and the adsorption tower A are substantially balanced, the program control valve is closed. 10A.
  • the program control valves 7A, 7B, 9A and 9B are opened, and the gas in the B tower enters the A tower through the pipes G19 and G17, and the two ends of the A tower are pressure-boosted (2E9R' for short).
  • the program-controlled valves 7B, 9A and 9B are closed.
  • the fifth step of pressure equalization at both ends referred to as the two ends of the two rises 2E5R'
  • the program-controlled valves 4A, 4H and 12H are opened.
  • the gas in the H tower enters the A tower through the pipelines G14 and G112, and the three-stage equalizing pressure is boosted at both ends (abbreviated as 2E3R').
  • the process control is closed 4H, 12A and 12H.
  • the program-controlled valves 41, 11A and 111 are opened, and the gas in the I tower enters the A tower through the pipelines G14 and G111, and the two-stage equalizing pressure boosting (2E2R') is performed on the A tower.
  • the process valves 4A, 41 and 111 are closed.
  • the a tower has completed the final step-up FR step, the program-controlled valves la, 2a are opened, and the intermediate mixed gas enters the adsorption tower a through the pipe G21, and in the adsorption column, the adsorbent selectively adsorbs the first-stage pressure swing adsorption device.
  • Carbon dioxide and other components in the outlet gas a small amount of carbon dioxide that is not adsorbed, and carbon monoxide that is not easily adsorbed, Methane, nitrogen, hydrogen and other components flow from the outlet end through the programmed valve 2a into the compression section of synthetic ammonia.
  • the total amount of carbon dioxide adsorbed by the adsorbent increases continuously.
  • the adsorbent adsorbs carbon dioxide
  • the carbon dioxide in the outlet gas The concentration is controlled below 0.2% (V)
  • the process control is closed, 2a, stop, and the intake is stopped. At this time, the adsorption is finished, and the process control is closed, 2a.
  • the program-controlled valves 3a, 3c are opened, and the gas in the a tower enters the c-tower through the pipe G23 to uniformly rise the c-tower.
  • the program-controlled valve 3a is closed.
  • the g tower is subjected to five equal rises.
  • the program control valves 5f and 5a are closed.
  • the program-controlled valves 6a, 6b are opened, and the gas in the b tower enters the a tower through the pipe G26 to perform a six-equal rise.
  • the program-controlled valves 6a, 6b are closed.
  • the gas in the d tower enters the a tower pair through the pipeline G25.
  • the a tower is subjected to four equal rises, and when the pressures of the d and a towers are substantially balanced, the program control valves 5a, 5d are closed.
  • the program control valve 4f is opened, and the gas in the f tower enters the a tower through the pipe G24 to perform the second equalization of the a tower.
  • the program control valves 4f, 4a are closed.
  • the first reverse pressure equalization step referred to as a uniform rise E1R
  • the program control valve 3a, 3g is opened, and the gas in the g tower enters the a tower through the pipeline G23.
  • the tower is uniformly raised.
  • the program control valve is closed 3g.
  • the program control valve KV-16 is opened, and the a tower is boosted from the top by the outlet gas of the adsorption tower in the adsorption step.
  • the program control valves KV-16, 3a are closed. .
  • the b ⁇ h adsorption tower is the same as the a-column cycle, except that it is staggered in time, as shown in Figures 2 and 3.
  • V The carbon dioxide, hydrogen, nitrogen and carbon monoxide recovery is greater than 99. 9% (V), the concentration of carbon dioxide in the product hydrogen and nitrogen is less than 0.2% (V) , tons of ammonia power consumption 2 degrees (instrument and lighting power).
  • the specific adsorbent combination of the present invention is employed, under other conditions (the adsorption pressure is
  • Embodiment 2 of the present invention is a diagrammatic representation of Embodiment 2 of the present invention.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 1 005MPa ⁇ The pressure of the carbon dioxide is 0. 005MPa.
  • the 12 adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption 10 times pressure equalization program is run.
  • the 8 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption six equal pressure program is run.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea.
  • the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the second stage of the pressure swing adsorption device is less than 0.8% (V), to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • both ends 5 E2D2E, 2E6D' at both ends, 2E7D' at both ends, 2E8D' at both ends, 2E9D' at both ends, 2E10D' at both ends, 2E10D' at both ends
  • Pressure BD two-stage gas boost 2ER, both ends are equal to 2E10R', both ends are equal to 2E9R', both ends are equal to 2E8R', both ends are increased by 2E7R', and both ends are raised by 2E6R', The two ends are equal to 2E5R', the two ends are 2E4R', the two ends are 5 liters 2E3R', the two ends are 2E2R', and both ends are 2E1 R', and the final boost FR pressure swing adsorption process
  • the gas obtained by the first stage pressure swing adsorption device in the product carbon dioxide reverse pressure reduction BD step is the product carbon dioxide, and the adsorption tower of the second stage pressure swing adsorption device
  • E2R, one 10 liters E1R, final boost FR pressure swing adsorption process step the second stage pressure swing adsorption device is in the adsorption step of the adsorption tower outlet A mixed gas of mainly nitrogen and hydrogen product, wherein carbon monoxide and further contains a small amount of methyl embankment.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the product carbon dioxide reverse buck BD adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • the specific adsorbent combination of the present invention is used in other conditions (adsorption pressure is 1. 8 MPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and 0 control function, dedicated In the same case of program-controlled valve and hydraulic system structure and life, the initial decarbonization investment can save 9%.
  • Embodiment 3 of the present invention is a diagrammatic representation of Embodiment 3 of the present invention.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the fifth embodiment is 005MPa ⁇ The pressure of the product is 0. 005MPa.
  • the 12 adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption 10 times pressure equalization program is run.
  • the 8 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption six equal pressure program is run.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea
  • the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that In the second stage of the pressure swing 0, the concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower is less than 0.2% (V), to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one average drop - E1D, two average drop E2D, three average drop E3D, four average drop E4D, five average drop E5D, six average drop E6D in one cycle. Seven equals
  • E7D both ends are reduced by 2E8D'
  • both ends are reduced by 2E9D '
  • both ends are reduced by 2E10D'
  • the product is oxidized by 5 carbon reverse buck BD
  • the second stage is boosted by 2ER
  • both ends are increased by 2E10R'
  • two End eight equals 2E8R', seven average E7R, six average E6R, five average E5R, four average E4R, three average E3R, two equal E2R, one equal E1R, final boost FR pressure swing adsorption process
  • the first stage pressure swing adsorption device in the product carbon dioxide reverse buck BD step of the gas obtained is the product carbon dioxide
  • the second stage of the pressure swing adsorption device adsorption tower in a cycle through the adsorption A
  • the second stage pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the product carbon dioxide reverse buck BD adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 3. OMPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and control functions, dedicated program control Valve and hydraulic system construction and life) Under the same conditions, the initial decarbonization investment can save 7%.
  • Embodiment 4 of the present invention is a diagrammatic representation of Embodiment 4 of the present invention.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 1 005MPa ⁇ The pressure of the carbon dioxide is 0. 005MPa.
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program
  • 6 adsorption towers constitute the second stage pressure swing adsorption device
  • the single tower adsorption four equal pressure program is run.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea
  • the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower of the second stage is less than 0.8% (V), to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • the second stage pressure swing adsorption device is in the adsorption step of the adsorption tower outlet to discharge the mixture mainly nitrogen, hydrogen products, which also contain a small amount of carbon monoxide and formamidine.
  • the second stage pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the product carbon dioxide reverse buck BD adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • V 8% (V ) 'T
  • the product has a carbon dioxide purity of 98% (V), a carbon dioxide, hydrogen, nitrogen and carbon monoxide recovery rate of more than 99. 5% (V) Ammonia consumes 2 degrees (electrical instrumentation and lighting).
  • the specific adsorbent combination of the present invention is employed, under other conditions (the adsorption pressure is
  • Embodiment 5 of the present invention .
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 0. 005MPa ⁇ The pressure of the carbon dioxide is 0. 005MPa.
  • the 12 adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption 10 times pressure equalization program is run.
  • the 6 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption three pressure equalization program is operated.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea, and the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower of the second stage of the pressure swing adsorption device is less than 0.2% (V) to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • the gas obtained by the first stage pressure swing adsorption device in the product carbon dioxide reverse step BD step and the vacuum VC step is the product carbon dioxide
  • the adsorption tower of the second stage pressure swing adsorption device is in a cycle
  • the adsorption is eight, one is E1 D, the second is E2D, the third is E3D, the reverse is BD, the vacuum is VC, the three is E3R, and the second is E2R, a liter of both E1 R
  • the final boosting FR pressure swing adsorption process step the second segment means is in a pressure swing adsorption gas mixture discharged from the adsorption column outlet of the adsorption step is mainly nitrogen, Hydrogen products, which also contain small amounts of carbon monoxide and methane.
  • the second stage of the pressure swing adsorption device adsorption tower reverse BD step and the vacuum VC step of the gas are all returned to the first stage of the pressure swing adsorption device has been completed and the vacuum VC step of the adsorption tower for boosting, referred to as two-stage gas boost 2ER .
  • the result of this example is that the carbon dioxide purity of the product is 98% (V), the carbon dioxide recovery rate is greater than 99% (V), the recovery of hydrogen, nitrogen and carbon monoxide is greater than 99.9% (V), and the concentration of carbon dioxide in the product hydrogen and nitrogen is less than 0. 2% (V), electricity consumption per ton of ammonia (meter and lighting).
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 0.6 MPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and control functions, dedicated program control Valve and hydraulic system construction and life) Under the same conditions, the initial decarbonization investment can save 12%.
  • Embodiment 6 of the present invention is a diagrammatic representation of Embodiment 6 of the present invention.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 0. 005MPa ⁇ The pressure of the carbon dioxide is 0. 005MPa.
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program
  • 6 adsorption towers constitute the second stage pressure swing adsorption device, and runs the single tower adsorption three pressure equalization program.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea
  • the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that In the second stage of the pressure swing adsorption device, the concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower is less than 0.2% (V), to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • the second stage of the pressure swing adsorption device is in the adsorption step of the adsorption tower outlet to discharge the main gas is mainly nitrogen, hydrogen products, which also contain a small amount of carbon monoxide and methane
  • the second stage of the pressure swing adsorption device adsorption tower reverse BD step and the vacuum VC step of the gas are all returned to the first stage of the pressure swing adsorption device has completed the vacuum VC adsorption tower for boosting, referred to as two-stage gas boost 2ER.
  • the result of this example is that the carbon dioxide purity of the product is 98% (V), carbon dioxide, hydrogen, nitrogen and one.
  • the carbon oxide recovery rate is greater than 99.9% (V)
  • the product carbon dioxide concentration in hydrogen and nitrogen is less than 0.2% (V)
  • the electricity consumption per ton of ammonia is 95 degrees (meter and lighting).
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 0.6 MPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and control functions, dedicated program control Valve and hydraulic system construction and life) Under the same conditions, the initial decarbonization investment can save 7%.
  • Embodiment 7 of the present invention is a diagrammatic representation of Embodiment 7 of the present invention.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 0. 005MPa ⁇ The pressure of the product is 0. 005MPa.
  • adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption process is carried out for 1 1 pressure equalization process.
  • the 7 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption four pressure equalization program is operated.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea, and the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower of the second stage of the pressure swing adsorption device is less than 0.2% (V) to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle. Seven average E7D, two ends are reduced by 2E8D', two ends are reduced by 2E9D', both ends are reduced by 2E10D', both ends are reduced by 2E11D', product carbon dioxide is reduced by BD, and two stages are boosted.
  • 2ER, 11E at both ends are 2E1 1R', 2E10R' at both ends, 2E9R' at both ends, 2E8R' at both ends, E7R at E6R, E6R at E6R, E6R at E6R , four equals E4R, three equals E3R, two equals E2R, one equals E1R, and finally boosts FR pressure swing adsorption process steps, the gas obtained by the first stage pressure swing adsorption device in the product carbon dioxide reverse buck BD step
  • the adsorption tower of the second stage pressure swing adsorption device undergoes adsorption A, one equal E1D, two equal E2D, three equal E3D, four equal E4D, reverse BD, vacuum in one cycle.
  • the second stage of the pressure swing adsorption device is in the adsorption step of the adsorption tower outlet to discharge the mixture is mainly nitrogen, hydrogen products, which also contain a small amount of carbon monoxide and methane.
  • the second stage of the pressure swing adsorption device adsorption tower reverse BD step and the vacuum VC step of the gas are all returned to the first stage of the pressure swing adsorption device has completed the product carbon dioxide reverse buck BD adsorption tower for boosting, referred to as two-stage gas boost 2ER.
  • the specific adsorbent combination of the present invention is employed, under other conditions (the adsorption pressure is 0. 8MPa (G), conversion gas composition and temperature, adsorption cycle time, power equipment performance, instrumentation and control functions, special program control valve and hydraulic system structure and life) Under the same circumstances, the decarbonization initial equipment investment can save 7 %.
  • Embodiment 8 of the present invention is a diagrammatic representation of Embodiment 8 of the present invention.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 0. 005MPa ⁇ The pressure of the carbon dioxide is 0. 005MPa.
  • adsorption towers are used to form the first stage pressure swing adsorption device, and the single tower adsorption process is carried out for 1 1 pressure equalization process.
  • the adsorption tower is composed of the second stage pressure swing adsorption device, and the single tower adsorption double pressure equalization program is operated.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea, and the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that In the second stage of the pressure swing adsorption device, the concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower is less than 0.2% (V), to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device undergoes adsorption A, one equal E1 D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • the second stage pressure swing adsorption device adsorbs the gas in the BD step. All return to the first stage of the pressure swing adsorption device has completed the vacuum pump step of the adsorption tower for boosting, referred to as two-stage gas boost 2ER.
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 0.6 MPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and control functions, dedicated In the same case of program-controlled valve and hydraulic system structure and life, the investment in decarbonization initial equipment can save 7%.
  • Embodiment 9 of the present invention The conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 0. 005MPa ⁇ The pressure of the carbon dioxide is 0. 005MPa.
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs a single tower adsorption 1 1 pressure equalization program
  • 5 adsorption towers constitute a second stage pressure swing adsorption device, and runs a single tower adsorption two pressure equalization program.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea, and the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower of the second stage of the pressure swing adsorption device is less than 0.2% (V) to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • both ends are reduced by 2E5D', the two ends are reduced by 2E6D', the two ends are reduced by 2E7D', the two ends are reduced by 2E8D', the two ends are reduced by 2E9D', and both ends are reduced by 2E10D', Both ends H ⁇ - average 2E11D', product dioxide reverse buck BD, two gas boost 2ER, both ends "one rise 2E11R", both ends rise 2E10F: ', both ends are 2E9R' 2E8R' at both ends, 2E7R' at both ends, 2E6R' at both ends, 2E5R' at both ends, 2E5R' at both ends, 2E4R' at both ends, 2E3R' at both ends, 2 The second phase is 2E2R', the two ends are both raised 2E1R', and the final step-up FR pressure swing adsorption process step, the gas obtained by the first stage pressure swing adsorption device in the product carbon dioxide reverse
  • Reverse BD, cleaning P, two equal E2R, one equal E1R, final boost FR pressure swing adsorption process step the mixture gas discharged in the PP step is directly cleaned by the flow adjustment to the adsorption tower that has completed the reverse BD step
  • the desorbed impurities on the adsorbent are desorbed, and the mixed gas discharged from the outlet of the adsorption tower in the second stage of the pressure swing adsorption device is mainly nitrogen and hydrogen products, which also contains a small amount of carbon monoxide and formamidine.
  • the pressure swing adsorption device of the adsorption tower adsorbs the BD step and the cleaning step P all return to the first stage of the pressure swing adsorption device has completed the product carbon dioxide D step down step of the adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • the specific adsorbent combination of the present invention is employed, under other conditions (the adsorption pressure is
  • Embodiment 10 of the present invention is a diagrammatic representation of Embodiment 10 of the present invention.
  • the composition of the shift gas, temperature, adsorbent type, power equipment performance, instrumentation and the like in this embodiment 005MPa ⁇
  • the pressure of the product is 0. 005MPa.
  • the pressure of the product is 0. 005MPa.
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program
  • 7 adsorption towers constitute the second stage pressure swing adsorption device
  • the single tower adsorption double pressure equalization program is run.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea
  • the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower of the second stage of the pressure swing adsorption device is less than 0.2% (V) to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • the mixture gas discharged from the PP2 step is directly cleaned by the flow rate adjustment to complete the cleaning tower of the P1 step.
  • the mixture gas discharged in the PP3 step is directly cleaned by the flow rate adjustment to the adsorption tower which has completed the reverse BD step, and the adsorbed impurities on the adsorbent are desorbed, and the second stage pressure swing adsorption device is in the adsorption step of the adsorption step.
  • the mixture discharged from the outlet is mainly nitrogen and hydrogen products, which also contain a small amount of carbon monoxide and methane.
  • the second stage pressure swing adsorption unit adsorption tower reverses the BD step and the gases for cleaning the P1, P2 and P3 steps all return to the first stage.
  • the pressure adsorption device has completed the adsorption of the product carbon dioxide reverse buck BD step, referred to as the second stage gas boost 2ER.
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 0.8 MPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and control functions, dedicated program control Valve and hydraulic system structure and life) Under the same conditions, the electricity consumption per ton of ammonia is reduced by 30%, and the investment in initial equipment for decarbonization can be saved by 7%.
  • adsorption pressure is 0.8 MPa (G)
  • conversion gas composition and temperature 0.8 MPa (G)
  • adsorption cycle time power plant performance
  • instrumentation and control functions dedicated program control Valve and hydraulic system structure and life
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the present embodiment is 005MPa ⁇ The pressure of the product is 0. 005MPa.
  • adsorption towers constitute the first stage of pressure swing adsorption device, running single tower adsorption 1 1 pressure equalization program, 7 adsorption towers constitute the second stage pressure swing adsorption device, running single tower adsorption two pressure equalization program.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea, and the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that 2% ( V), to meet the stability of the hydrogen and nitrogen in the second stage of the pressure swing adsorption device
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle. Seven averages drop E7D, both ends are reduced by 2E8D', both ends are reduced by 2E9D', both ends are reduced by 2E 10D', both ends are H "" - both fall 2E1 1D', product carbon dioxide reverse buck BD, two Segment gas boost 2ER, both ends eleven rise 2E1 1 R',
  • the gas obtained in the step is the product carbon dioxide.
  • the adsorption tower of the second stage pressure swing adsorption device successively undergoes adsorption A in one cycle, E1D in one drop, E2D in E2D, PP1 in the same direction, and PP2 in the same direction.
  • 0 PP3, reverse BD, cleaning Pl, cleaning P2, cleaning P3, two equalizing E2R, one equalizing E1 R, final boosting FR pressure swing adsorption process step, and the mixture gas discharged by the PP1 step is directly passed through the flow regulation.
  • the mixed gas directly removes the adsorption 5 tower which has completed the reverse BD step by flow regulation, and desorbs the adsorbed impurities on the adsorbent, and the second-stage pressure swing adsorption device is in the adsorption step of the adsorption tower outlet of the adsorption step.
  • a nitrogen and hydrogen product which also contains a small amount of carbon monoxide and
  • the carbon dioxide concentration of the product is less than 0. 2% (V)
  • the carbon dioxide, hydrogen, nitrogen, and carbon monoxide recovery is greater than 99.9% (V).
  • the electricity consumption per ton of ammonia is 2 degrees.
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 0.9 MPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation, and 5 control functions, Special program-controlled valve and hydraulic system structure and life) Under the same conditions, the electricity consumption per ton of ammonia decreases 30%, the initial equipment investment in decarbonization can save 7%.
  • Embodiment 12 of the present invention is a diagrammatic representation of Embodiment 12 of the present invention.
  • the raw material gas in this example is a hydrogen-containing gas mixture, such as light oil gas, synthetic ammonia shift gas, syngas, synthetic ammonia gas, methanol synthesis gas, semi-water gas, water gas, cracked dry gas, etc.
  • a hydrogen-containing gas mixture such as light oil gas, synthetic ammonia shift gas, syngas, synthetic ammonia gas, methanol synthesis gas, semi-water gas, water gas, cracked dry gas, etc.
  • the adsorbent of the first stage of the pressure swing adsorption gas separation device in the adsorption tower from bottom to top is activated alumina and fine pore silica gel or activated alumina and activated carbon or activated alumina, activated carbon and molecular sieve; the second stage pressure swing adsorption In the gas separation device, the adsorbent packed in the adsorption tower is activated carbon and molecular sieve or molecular sieve.
  • the present embodiment is a pressure swing adsorption hydrogen production device.
  • hydrogen is a component which is difficult to adsorb phase, and a component other than hydrogen is an easily adsorbable phase component.
  • the first stage of the pressure swing adsorption gas separation device of the present embodiment adsorbs.
  • the hydrogen outlet of the column is controlled to be above 80% (V), and the component of the easily adsorbable phase is concentrated to 97% (V) or more, so that the hydrogen content is less than 0.6% (V), and the second stage pressure swing adsorption gas separation device
  • the 9% (V) the concentration of the hydrogen in the outlet of the second stage of the pressure swing adsorption gas separation device is greater than 99.9% (V), To meet the needs of the next step.
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program, 6 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption four equal pressure program is run.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • both ends are reduced by 2E5D', the two ends are reduced by 2E6D', the two ends are reduced by 2E7D', the two ends are reduced by 2E8D', the two ends are reduced by 2E9D', and both ends are reduced by 2E10D', Both ends H ⁇ - decrease 2E1 1D', reverse buck BD, two-stage gas boost 2ER, both ends H ⁇ - rise 2E1 1R', both ends rise 2E10R', both ends rise 2E9R', Both ends are 8E2R', both ends are 2E7R', 6E are 2E6R' at both ends, 2E5R' at both ends are raised, 2E4R' is raised at both ends, and 2E3R' is raised at both ends.
  • E2R, L are E1R
  • the second segment swing adsorption apparatus are in the product gas discharged from the outlet of the adsorption tower of the adsorption step is mainly hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage pressure swing adsorption device
  • the adsorption tower of the reverse buck BD is completed to perform boosting, which is referred to as two-stage gas boosting 2ER.
  • the result of this example is that the hydrogen concentration is greater than 99.9% (V) and the hydrogen recovery is greater than 99% (V).
  • Embodiment 13 of the present invention is a diagrammatic representation of Embodiment 13 of the present invention.
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program control valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 1. 8MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program, 5 adsorption towers constitute the second stage pressure swing adsorption device, and runs the single tower adsorption three equal pressure program.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • both ends are reduced by 2E5D', the two ends are reduced by 2E6D', the two ends are reduced by 2E7D', the two ends are reduced by 2E8D', the two ends are reduced by 2E9D', and both ends are reduced by 2E10D',
  • Both ends H "-all decrease 2E1 1D', reverse buck BD, two-stage gas boost 2ER, both ends H"-average 2E11R', both ends are equal to 2E10R', both ends are equal to 2E9R', two 8E rises to 2E8R', 7E rises at both ends, 2E7R', 6E rises at both ends, 2E6R', 5E rises at both ends, 2E5R', both ends rise 2E4R', both ends rise 2E3R', both ends Both rise 2E2R', both ends are raised 2E1 R ', the final step-up FR pressure swing adsorption process step, the first stage pressure swing adsorption process
  • the product gas discharged from the outlet of the adsorption tower at the second stage of the pressure swing adsorption device is mainly hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the reverse pressure reduction BD adsorption tower to boost, referred to as the second stage gas boost 2ER.
  • the result of this example is that the hydrogen concentration is greater than 99% (V) and the hydrogen recovery is greater than 98% (V).
  • Embodiment 14 of the present invention is a diagrammatic representation of Embodiment 14 of the present invention.
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program, 6 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption four equal pressure program is run.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one average drop in one cycle
  • the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the reverse pressure reduction BD adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • the result of this example is that the hydrogen concentration is greater than 99.9% (V) and the hydrogen recovery is greater than 99% (V).
  • Embodiment 15 of the present invention is a diagrammatic representation of Embodiment 15 of the present invention.
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program control valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 1. 8MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program, 5 adsorption towers constitute the second stage pressure swing adsorption device, and runs the single tower adsorption three equal pressure program.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one average drop in one cycle
  • the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the stage pressure swing adsorption device is mainly hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas all return to the first stage of the pressure swing adsorption device has completed the reverse pressure reduction BD adsorption tower for boosting, referred to as two-stage gas boost 2ER.
  • the result of this example is that the hydrogen concentration is greater than 99% (V) and the hydrogen recovery is greater than 98% (V).
  • Embodiment 16 of the present invention is a diagrammatic representation of Embodiment 16 of the present invention.
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. . 5MPa ( G ).
  • the 12 adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption 10 times pressure equalization program is run.
  • the 5 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption double pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device sequentially undergoes adsorption A in one cycle, and both ends Both are 2E1D', 2E2D' at both ends, 2E3D' at both ends, 2E4D' at both ends, 2E5D' at both ends, 2E6D' at both ends, and 7E at both ends 2E7D ', both ends are reduced by 2E8D ', both ends are reduced by 2E9D', both ends are reduced by 2E10D', reverse buck BD, vacuum VC:, two-stage gas boost 2ER, both ends are equal to 2E10R ', 9E on both ends is 2E9R', 8E on both ends is 2E8R', 7E on both ends is 2E7R', 6E on both ends is 2E6R', 5E on both ends is 2E5R', and both ends are 2E4R'.
  • the two ends are increased by 2E3R', the two ends are both raised by 2E2R', the two ends are both raised by 2E1 R', and the final stepped FR pressure swing adsorption process step is obtained by the first stage pressure swing adsorption device in the reverse step-down BD step.
  • the gas is vented or used.
  • the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A, one equal E1D, two equal E2D, reverse BD, vacuum VC, two equal E2R, one cycle in one cycle.
  • the E1 R and the final boost FR pressure swing adsorption process steps, and the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverse BD step and the vacuum VC step of the gas are all returned to the first stage of the pressure swing adsorption device has completed the reverse pressure reduction BD adsorption tower for boosting, referred to as two-stage gas boost 2ER .
  • Example 17 of the present invention is that the hydrogen concentration is greater than 99% (V) and the hydrogen recovery is greater than 99.5% (V) o
  • Example 17 of the present invention is that the hydrogen concentration is greater than 99% (V) and the hydrogen recovery is greater than 99.5% (V) o
  • Example 17 of the present invention is that the hydrogen concentration is greater than 99% (V) and the hydrogen recovery is greater than 99.5% (V) o
  • Example 17 of the present invention is that the hydrogen concentration is greater than 99% (V) and the hydrogen recovery is greater than 99.5% (V) o
  • V 99%
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. . 5MPa (G).
  • 13 adsorption towers constitute the first stage pressure swing adsorption device, run a single tower adsorption 11 times pressure equalization program, 5 adsorption towers constitute a second stage pressure swing adsorption device, run a single tower adsorption two pressure equalization program
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • E7D Seven average E7D, two ends are reduced by 2E8D', two ends are reduced by 2E9D', both ends are reduced by 2E10D', both ends are reduced by 2E11D', reverse buck BD, vacuum VC, two gas Boost 2ER, both ends H ⁇ - 2E1 1 R', 2E10R' at both ends, 2E9R' at both ends, 2E8R' at both ends, E7R at 7E, E6R at 6E, Wujunsheng E5R, Sijunsheng E4R, Sanjunsheng E3R, Erjunsheng E2R, Yijunsheng E1R, final boost FR pressure swing adsorption process step, the first stage pressure swing adsorption device obtained in the reverse buck BD step The gas is vented or used.
  • the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A, one equal E1D, two equal E2D, reverse BD, vacuum VC, and two equal E2R in one cycle.
  • a uniform E1 R, final boost FR pressure swing adsorption process step the second stage pressure swing adsorption device is in adsorption Discharged from the adsorption column outlet gas main product quench hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas all return to the first stage of the pressure swing adsorption device has completed the reverse pressure reduction BD and vacuum VC adsorption tower for boosting, referred to as two-stage gas boost 2ER.
  • the result of the present embodiment is that the hydrogen concentration is greater than 99% (V), and the hydrogen recovery rate is greater than 99.5% (V).
  • Embodiment 18 of the present invention The conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. . 5MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program, 7 adsorption towers form the second stage pressure swing adsorption device, and runs the single tower adsorption four times pressure equalization program.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A, one equal E1D, two equal E2D, three equal E3D, four equal E4D, and reverse BD in one cycle.
  • vacuum pumping VC four average E4R, three average E3R, two equal E2R, one equal E1R, final boost FR change
  • the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly hydrogen gas.
  • the second stage pressure swing adsorption device adsorption tower reverses the BD step gas all back to the first stage pressure swing adsorption •
  • the device has been boosted by an adsorption tower that performs reverse buck BD and vacuum VC steps, referred to as two-stage gas boost 2ER.
  • the result of the present embodiment is that the hydrogen concentration is greater than 99% (V), and the hydrogen recovery rate is greater than 99.5% (V).
  • Embodiment 19 of the present invention is a diagrammatic representation of Embodiment 19 of the present invention.
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. . 5MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, run single tower adsorption 1 1 pressure equalization program, 4 adsorption towers constitute the second stage pressure swing adsorption device, run single tower adsorption two pressure equalization program
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • E7D Seven average E7D, two ends are reduced by 2E8D', two ends are reduced by 2E9D', both ends are reduced by 2E10D', both ends are reduced by 2E1 1D', reverse buck BD, vacuum VC, two Segment gas boost 2ER, both ends H "" - 2E11R', both ends are 2E10R', both ends are 2E9R', both ends are 8E8R', 7E are E7R, 6E are E6R , Wujunsheng E5R, Sijunsheng E4R, Sanjunsheng E3R, Erjunsheng E2R, Yijunsheng E1R, final boost FR pressure swing adsorption process steps, the first stage pressure swing adsorption device obtained in the reverse buck BD step The gas is vented or used.
  • the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A, one equal E1D, two equal E2D, reverse BD, two equal E2R, and one E1R in one cycle.
  • final boost FR In the pressure swing adsorption process step, the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the reverse pressure reduction BD adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • the result of the present embodiment is that the hydrogen concentration is greater than 99% (V), and the hydrogen recovery rate is greater than 99.5% (V).
  • Embodiment 20 of the present invention is a diagrammatic representation of Embodiment 20 of the present invention.
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. 8MPa (G).
  • adsorption towers are composed of the first stage pressure swing adsorption device, and the single tower adsorption U times pressure equalization program is run.
  • the five adsorption towers constitute the second stage pressure swing adsorption unit, and the single tower adsorption double pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one average drop in one cycle
  • the second section is in the pressure swing adsorption means is discharged in the adsorption column outlet gas of the adsorption step is mainly hydrogen product.
  • the second stage of the pressure swing adsorption unit adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device.
  • the reverse pressure reduction BD and vacuum pumping step of the adsorption tower have been completed, referred to as the second stage gas boost 2ER.
  • Example 21 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery is greater than 99.8% (V) o
  • Example 21 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery is greater than 99.8% (V) o
  • Example 21 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery is greater than 99.8% (V) o
  • Example 21 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery is greater than 99.8% (V) o
  • V hydrogen concentration is greater than 99.9% (V)
  • V hydrogen recovery is greater than 99.8%
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. ⁇ 8MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, run single tower adsorption 1 1 pressure equalization program, 7 adsorption towers constitute the second stage pressure swing adsorption device, run single tower adsorption two pressure equalization program
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1 D ' at both ends, 2E2D ' at both ends, 2E3D' at both ends, and 4E at both ends.
  • the tower undergoes adsorption A, E1D, E2D, PP2, PP2, PP3, BD, P1, P2, P2, C6, C3, 2, and 2 in a cycle.
  • E2R one equal E1R
  • final boost FR pressure swing adsorption process step the mixture gas discharged in the PP1 step is directly cleaned by the flow adjustment to clean the adsorption tower that has completed the cleaning P2 step, so that it is sucked
  • the adsorbed impurities on the agent are desorbed, and the mixture gas discharged from the PP2 step is directly cleaned by the flow rate adjustment to the adsorption tower which has completed the cleaning P1 step, and the mixture gas discharged by the PP3 step is directly cleaned by the flow rate adjustment and has been completed.
  • the adsorption tower of the step desorbs the adsorbed impurities on the adsorbent, and the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly hydrogen.
  • the second stage pressure swing adsorption device is reversed by the adsorption tower.
  • the gas in the BD step is all returned to the adsorption tower of the first stage pressure swing adsorption device that has completed the reverse pressure reduction BD and the vacuum VC step, and is referred to as the second stage gas pressure boost 2ER.
  • Embodiment 22 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99.8% (V).
  • Embodiment 22 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99.8% (V).
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. . 9MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, run a single tower adsorption 11 times pressure equalization program, 7 adsorption towers constitute a second stage pressure swing adsorption device, run a single tower adsorption two pressure equalization program
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one average drop in one cycle
  • E1D two average E2D, three average E3D, four average E4D, five average E5D, six average E6D, seven average E7D, two ends are reduced by 2E8D', both ends are reduced by 2E9D', both ends Decimal 2E10D', both ends - one down 2E11D', reverse buck BD, two-stage gas boost 2ER, both ends H "" - both rise 2E11R', both ends rise 2E10R', both ends 2E9R', 2E8R' at both ends, 7 E8R, 6 E, E6R, E5R, E4R, E4R, E2R, E2R, E1R, Final boost
  • the gas obtained by the first stage pressure swing adsorption device in the reverse pressure reduction BD step is vented or used, and the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A and one time in one cycle.
  • the mixture gas discharged from the PP1 step is directly cleaned by the flow adjustment to clean the adsorption tower that has completed the cleaning P2 step, so that The adsorbed impurities on the adsorbent are desorbed, and the mixture gas discharged by the PP2 step is directly cleaned by the flow rate adjustment to complete the adsorption tower of the P1 step, and the mixture gas discharged by the PP3 step is directly cleaned by the flow rate adjustment.
  • the adsorption tower of the BD step is reversed to desorb the adsorbed impurities on the adsorbent, and the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the reverse pressure reduction BD and vacuum VC step of the adsorption tower for boosting, referred to as two-stage gas boost 2ER.
  • Embodiment 23 of the present invention is that the hydrogen concentration is greater than 99. 9 ° /. (V), the hydrogen recovery rate is greater than 99.8% (V).
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 3 005MPa ⁇ The pressure of the product is 0. 005MPa.
  • the 12 adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption 10 times pressure equalization program is run.
  • the 8 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption six equal pressure program is run.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to 98.5% (V) or more for synthesizing urea
  • the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device.
  • the concentration of carbon dioxide in the hydrogen and nitrogen in the outlet of the second stage of the pressure swing adsorption device is less than 0.2% (V), to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device undergoes adsorption A, one equal E1 D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • Reverse gas reduction BD1 step gas return The first stage pressure swing adsorption gas separation device boosts the adsorption tower from the bottom, and the gas obtained by the first stage pressure swing adsorption device in the product carbon dioxide reverse pressure reduction two BD2 step is a product. Carbon dioxide, the adsorption tower of the second stage pressure swing adsorption device undergoes adsorption A, one equal E1 D, two average E2D, three average E3D, four average E4D, five average E5D, and six averages in one cycle.
  • the mixture of the pressure swing adsorption device at the outlet of the adsorption tower which is in the adsorption step is mainly a nitrogen and hydrogen product, which also contains a small amount of carbon monoxide and methane.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the product carbon dioxide reverse pressure drop two BD2 adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • V The carbon dioxide, hydrogen, nitrogen and carbon monoxide recovery is greater than 99.9% (V), the concentration of carbon dioxide in the product hydrogen and nitrogen is less than 0.2% (V). , tons of ammonia power consumption 2 degrees (instrument and lighting power).
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 3. OMPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and control functions, dedicated program control Valve and hydraulic system construction and life) Under the same conditions, the initial decarbonization investment can save 7%.
  • Embodiment 24 of the present invention is a diagrammatic representation of Embodiment 24 of the present invention.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 0. 005MPa ⁇ The pressure of the carbon dioxide is 0. 005MPa.
  • the 12 adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption 10 times pressure equalization program is run.
  • the 6 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption three pressure equalization program is operated.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea, and the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that In the second stage of the pressure swing adsorption device, the concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower is less than 0.2% (V), to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one average drop in one cycle
  • E1D two average E2D, three average E3D, four average E4D, five average E5D, six average E6D, seven average E7D, eight average E8D, nine average E9D, ten average E10D, reverse buck One BD1, product carbon dioxide reverse pressure reduction two BD2, vacuum V (:, one gas boost 2ER1, two gas boost 2ER, ten average E10R, nine average E9R, eight average E8R, seven average E7R, Six average E6R, five average E5R, four average E4R, three average E3R, two equal E2R, one equal E1R, final boost FR pressure swing adsorption process, after the end of E10D, the adsorption tower
  • concentration of the carbon dioxide component at the top is greater than 70V%; the concentration of carbon dioxide at the bottom of the adsorption tower after the reverse depressurization-BD1 is greater than 75V%, and the gas of the reverse depressurization-BD1 step is returned to the first stage of the pressure swing
  • the adsorption tower of the second stage pressure swing adsorption device undergoes adsorption A, one equal E1 D, two equal E2D, three equal E3D, reverse BD, vacuum VC in one cycle;
  • the E3R, the two-elevation E2R, the one-elevation E1R, and the final step-up FR pressure swing adsorption process step, and the second-stage pressure swing adsorption device is in the adsorption step, and the mixture gas discharged from the adsorption tower outlet is mainly a nitrogen and hydrogen product, wherein It also contains a small amount of carbon monoxide and formazan.
  • the second stage of the pressure swing adsorption device adsorption tower reverse BD step and the vacuum VC step of the gas are all returned to the first stage of the pressure swing adsorption device has been completed and the vacuum VC step of the adsorption tower for the rise Pressure, referred to as the second stage gas boost 2ER.
  • the result of this example is that the carbon dioxide purity of the product is 98% (V), and the carbon dioxide recovery rate is greater than 99%.
  • V hydrogen, nitrogen and carbon monoxide recovery rate is greater than 99.9% (V)
  • product hydrogen nitrogen carbon dioxide concentration is less than 0.2% (V)
  • ton ammonia power consumption is 95 degrees (meter and lighting power).
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 5 0.6 MPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and control functions, dedicated program control Valve and hydraulic system construction and life) Under the same conditions, the initial decarbonization investment can save 12%.
  • Embodiment 25 of the present invention is a diagrammatic representation of Embodiment 25 of the present invention.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the 0 control function, the special program control valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is the same.
  • the delivery pressure of the product carbon dioxide is 0.005 MPa.
  • adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption 11 pressure equalization program is run. Seven adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption four equal pressure program is run.
  • the carbon dioxide is purified to 98% (V) or more for synthesizing urea
  • the second stage of the pressure swinging device is to further purify the outlet gas of the first stage pressure swing adsorption device.
  • the concentration of carbon dioxide in hydrogen and nitrogen at the outlet of the upper end of the adsorption tower of the second stage pressure swing adsorption device is less than 0.2°/. (V) to meet the needs of the next step in the synthesis of ammonia.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • the pressure swing adsorption gas separation device boosts the adsorption tower from the bottom, and the first stage pressure swing adsorption device is reversed in the product carbon dioxide. Gas obtained by stepping down the second BD2 step That is, the carbon dioxide of the product, the adsorption tower of the second stage pressure swing adsorption device undergoes adsorption A, one equal E1D, two equal E2D, three equal E3D, four equal E4D, reverse BD, pumping in one cycle.
  • Vacuum VC four equals 0 E4R, three equals E3R, two equalized E2R, one equalized E1R, and finally boosted FR pressure swing adsorption process step
  • the second stage pressure swing adsorption device is in the adsorption step of the adsorption tower outlet
  • the mixture gas is mainly nitrogen and hydrogen products, which also contain a small amount of carbon monoxide and methane.
  • the second stage pressure swing adsorption device adsorption tower reverse BD step and vacuum VC step gas all return to the first stage pressure swing adsorption device has been completed Product 2" Carbon oxide reverse buck BD adsorption tower for boosting, referred to as two-stage gas boost 2ER.
  • the result of this example is that the carbon dioxide purity of the product is 98% (V), carbon dioxide, hydrogen, nitrogen and one.
  • the carbon oxide recovery rate is greater than 99.9% (V)
  • the product hydrogen and nitrogen carbon dioxide concentration is less than 0.2% (V)
  • the ammonia power consumption is 65 degrees (meter and lighting power).
  • the specific adsorbent combination of the present invention is used under other conditions (adsorption pressure is 0.8 MPa (G), conversion gas composition and temperature, adsorption cycle time, power plant performance, instrumentation and control functions, dedicated program control ⁇ and hydraulic system structure and life) Under the same circumstances, the initial decarbonization investment can save 7%.
  • Embodiment 26 of the present invention : '
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program control width, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 0. 005MPa ⁇ The pressure of the carbon dioxide is 0. 005MPa.
  • adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption process is carried out for 1 1 pressure equalization process.
  • the 4 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption double pressure equalization program is operated.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea, and the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower of the second stage of the pressure swing adsorption device is less than 0.2% (V) to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device undergoes adsorption A, one equal E1 D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • the concentration of carbon dioxide at the top of the adsorption tower is greater than 70V%;
  • the concentration of carbon dioxide at the bottom of the adsorption tower is greater than 75V%, and the gas of the reverse pressure reduction-BD1 step is returned to the first stage of the pressure swing adsorption gas separation device to boost the adsorption tower from the bottom, and the first stage pressure swing adsorption device
  • the gas obtained in the vacuum VC step is the product carbon dioxide
  • the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A, one equal E1D, two equal E2D, reverse BD, and two equal E2R in one cycle.
  • the conditions of the reforming gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the embodiment are completely the same as those of the first embodiment, and the adsorption pressure of the embodiment is 0. 005MPa ⁇ The pressure of the product is 0. 005MPa.
  • adsorption towers constitute the first stage pressure swing adsorption device, running single tower adsorption 1 1 pressure equalization program, ⁇
  • Ten adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption double pressure equalization program is operated.
  • the first stage pressure swing adsorption device of the present embodiment purifies carbon dioxide to above 98% (V) for synthesizing urea
  • the second stage pressure swing adsorption device further purifies the outlet gas of the first stage pressure swing adsorption device, so that The concentration of carbon dioxide in the hydrogen and nitrogen at the outlet of the adsorption tower of the second stage of the pressure swing adsorption device is less than 0.2% (V) to meet the needs of the next step of ammonia synthesis.
  • the adsorption tower of the first stage pressure swing adsorption device undergoes adsorption A, one average drop in one cycle.
  • the gas obtained by the first stage pressure swing adsorption device in the product carbon dioxide reverse pressure reduction two BD2 step is the product dioxon 5 carbon
  • the adsorption tower of the second stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two equal E2D, a PP1, a PP2, a PP3, a reverse BD, a cleaning Pl, and a PB in a cycle.
  • the adsorbed impurities on the adsorbent are desorbed, and the mixture gas discharged from the PP2 step is directly cleaned by the flow rate adjustment 0.
  • the adsorption tower that has been cleaned in the P1 step is cleaned, and the mixture gas discharged in the PP3 step is directly passed through the flow adjustment.
  • Cleaning the adsorption tower that has completed the reverse BD step to dissolve the adsorbed impurities on the adsorbent
  • the mixture that is sucked out, the second stage of the pressure swing adsorption device is in the adsorption step of the adsorption tower outlet is mainly nitrogen and hydrogen products, which also contain a small amount of carbon monoxide and formazan.
  • the second stage of the pressure swing adsorption device adsorption tower reverse BD step and the cleaning of the P1, P2 and P3 steps all return to the first stage of the pressure swing adsorption device 5 has completed the product carbon dioxide reverse pressure reduction two BD2 step of the adsorption tower to boost, Abbreviated as two-stage airlift Press 2ER.
  • the specific adsorbent combination of the present invention is used in other conditions (the adsorption pressure is
  • Embodiment 28 of the present invention is a diagrammatic representation of Embodiment 28 of the present invention.
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the embodiment is 3. 0MPa (G).
  • 12 adsorption towers constitute the first stage pressure swing adsorption device, run a single tower adsorption 10 times pressure equalization program, 8 adsorption towers constitute a second stage pressure swing adsorption device, and run a single tower adsorption six times pressure equalization program
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one average drop in one cycle
  • E1D two average E2D, three average E3D, four average E4D, five average E5D, six average E6D, seven average E7D, eight average E8D, nine average E9D, ten average E10D, reverse buck One BD1, reverse bucking two BD2, one gas boost 2ER1, two gas boost 2ER, ten average E10R, nine average E9R, eight average E8R, seven average E7R, six average E6R, five average E5R, four-elevation E4R, three-elevation E3R, two-elevation E2R, one-elevation E1R, final boost FR pressure swing adsorption process step, after the end of E10D, the concentration of the easily adsorbable phase at the top of the adsorption tower is greater than 70W .
  • the concentration of the easily adsorbable phase at the bottom of the adsorption tower is greater than 75V%, and the gas of the reverse depressurization-BD1 step is returned to the first stage of the pressure swing adsorption gas separation device to boost the adsorption tower from the bottom, and the reverse is lowered.
  • the gas of the second BD2 is vented or used.
  • the adsorption tower of the second stage pressure swing adsorption device successively undergoes adsorption A in one cycle, E1 D, E2D, E3D, E4D, E4D , five average E5D, six average E6D, reverse BD, six average E6R, five average E5R, four average E4R, three average E3R, two average E2R, one equal E1 R, final boost FR
  • the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly hydrogen.
  • the second stage pressure swing adsorption unit adsorption tower reverses the BD step gas back to the first stage.
  • the pressure swing adsorption unit has completed the reverse pressure reduction two BD2 step of the adsorption tower for boosting, referred to as the second stage gas lift pressure 2ER.
  • Embodiment 29 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99.8% (V).
  • Embodiment 29 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99.8% (V).
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. 7MPa (G).
  • 12 adsorption towers constitute the first stage pressure swing adsorption device, run a single tower adsorption 10 times pressure equalization program
  • 6 adsorption towers constitute a second stage pressure swing adsorption device, run a single tower adsorption three pressure equalization program
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • the gas in the reverse step-down step BD1 is returned to the first stage of the pressure swing adsorption gas separation device to boost the adsorption tower from the bottom, and the gas of the reverse pressure drop two BD2 is vented or used, and the adsorption tower of the second stage pressure swing adsorption device is In a cycle, it goes through the adsorption A, and the average decreases.
  • Embodiment 30 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99. 9°/. (V).
  • Embodiment 30 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99. 9°/. (V).
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. 8MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, which runs the single tower adsorption 1 1 pressure equalization program, 7 adsorption towers form the second stage pressure swing adsorption device, and runs the single tower adsorption four times pressure equalization program.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A, one average drop in one cycle
  • E1D two average E2D, three average E3D, four average E4D, five average E5D, six average E6D, seven average E7D, eight average E8D, nine average E9D, ten average E10D, ⁇ "Eallly drop E1 1D, reverse buck one BD1, reverse buck two BD2, one gas boost 2ER1, two gas boost 2ER, H"" one rise E1 1 R, ten average rise E 10R, nine average ⁇ E9R, eight average E8R, seven average E7R, six average E6R, five average E5R, four average E4R, three average E3R, two equal E2R, one equal E1 R, final boost FR transformer
  • the concentration of the easily adsorbable phase at the top of the adsorption tower is greater than 70V%; after the end of the reverse depressurization-BD1, the concentration of the readily adsorbable phase at the bottom of the adsorption tower
  • the gas in the BD1 step is returned to the first stage of the pressure swing adsorption gas separation device to pressurize the adsorption tower from the bottom, reversely depressurize the gas of the second BD2 or use it, and the adsorption tower of the second stage pressure swing adsorption device is in a cycle In turn, it undergoes adsorption A, E1D, E2D, E2D, E3D, E4D, BD, vacuum VC;, four average E4R, three average E3R, two equal E2R, one equal E1 R, final boost FR pressure swing adsorption process step, the second stage pressure swing adsorption device is in the adsorption step of the adsorption tower outlet
  • the product gas is mainly hydrogen.
  • the second stage of the pressure swing adsorption device adsorption tower reverses the BD step gas back to the first stage of the pressure swing adsorption device has completed the reverse pressure reduction two BD2 step of the adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • Embodiment 31 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99.9% (V).
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program-controlled valve, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. 6MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption process is carried out for 1 1 pressure equalization process.
  • the 4 adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption double pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device undergoes adsorption A, one equal E1 D, two average E2D, three average E3D, four average E4D, five average E5D, and six E6D in one cycle.
  • the concentration of the easily adsorbable phase at the bottom of the adsorption tower is greater than 75V%, and the gas of the reverse depressurization-BD1 step returns to the first stage of the pressure swing adsorption gas separation device to pressurize the adsorption tower from the bottom, reverse
  • the gas of the second step BD2 is vented or used, and the second stage of pressure swing adsorption
  • the adsorption tower sequentially undergoes adsorption A, one equal E1D, two equal E2D, reverse BD, two equal E2R, one equal E1 R, and a final boost FR pressure swing adsorption process step in one cycle.
  • the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the adsorption pressure swinging device is mainly hydrogen.
  • the second stage of the pressure swing adsorption device is reversed, and the gas in the BD step is returned to the first stage of the pressure swing adsorption device.
  • the adsorption tower of the VC step performs boosting, referred to as the second-stage gas boosting 2ER.
  • Embodiment 32 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99.9% (V).
  • the conditions of the raw material gas composition, the temperature, the adsorbent type, the power equipment performance, the instrumentation and the control function, the special program control width, the hydraulic system structure and the service life of the present embodiment are completely the same as those of the embodiment 12, and the adsorption pressure of the present embodiment is 0. 6MPa (G).
  • adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption 1 1 pressure equalization program is run.
  • the 7 adsorption towers form the second stage pressure swing adsorption device, and the single tower adsorption double pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device sequentially undergoes adsorption A and average reduction in one cycle.
  • the stage pressure swing adsorption gas separation device boosts the adsorption tower from the bottom, reversely depressurizes the gas of the second BD2 or uses it, and the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A and one average in one cycle.
  • the adsorption tower of the BD step desorbs the adsorbed impurities on the adsorbent, and the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly hydrogen.
  • the second stage pressure swing adsorption device adsorbs the tower reverse
  • the gas in the BD step is returned to the first stage of the pressure swing adsorption device to complete the reverse pressure reduction of the second BD2 step of the adsorption tower for boosting, referred to as the second stage gas boost 2ER.
  • Embodiment 33 of the present invention is that the hydrogen concentration is greater than 99.9% (V), and the hydrogen recovery rate is greater than 99.8% (V).
  • the raw material gas in this case is air.
  • the first stage of the pressure swing adsorption gas separation device, the bottom-up loading adsorbent in the adsorption tower is activated alumina and molecular sieve in turn; the second stage pressure swing adsorption gas separation device, in the adsorption tower
  • the loaded adsorbent is a molecular sieve.
  • This embodiment is a pressure swing adsorption oxygen generator. In the air, oxygen and argon are components of the difficult phase to be adsorbed, and nitrogen and water (steam) are components of the easily adsorbable phase.
  • the first stage of the pressure swing adsorption gas separation in this embodiment The nitrogen adsorption of the outlet of the adsorption tower of the device is controlled at 78% (V) (in actual operation, it can also be adjusted between 30 and 78V%), and the second stage of the pressure swing adsorption gas separation device functions as the first stage pressure swing adsorption gas separation device.
  • the nitrogen in the outlet gas is further purified, so that the oxygen concentration at the outlet of the adsorption tower of the second stage of the pressure swing adsorption gas separation device is greater than 93% (V), up to 95V%, to meet the needs of the next step.
  • Seven adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption four-time pressure equalization program is run.
  • Four adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption one-time pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A, one equalization E 1 D, reverse pressure reduction BD, one equalization E1R, and finally boosted FR pressure swing adsorption process in one cycle.
  • the gas in the reverse step-down BD step enters the adsorption tower of the first stage pressure swing adsorption device to boost the adsorption tower that has completed the vacuum pumping, and the second stage pressure swing adsorption device is in the adsorption step of the adsorption tower outlet.
  • the gas is mainly oxygen and a small amount of argon.
  • the result of this example is that the oxygen concentration is greater than 93% (V) and the nitrogen concentration is greater than 99°/. (V), the oxygen recovery is greater than 96.2% (V).
  • Embodiment 34 of the present invention is a diagrammatic representation of Embodiment 34 of the present invention.
  • the raw material gas in this case is air.
  • the first stage of the pressure swing adsorption gas separation device, the bottom-up loading adsorbent in the adsorption tower is activated alumina and molecular sieve in turn; the second stage pressure swing adsorption gas separation device, in the adsorption tower
  • the loaded adsorbent is a molecular sieve.
  • This embodiment is a pressure swing adsorption oxygen generator. In the air, oxygen and argon are components of the difficult phase to be adsorbed, and nitrogen and water (steam) are components of the easily adsorbable phase.
  • the first stage of the pressure swing adsorption gas separation in this embodiment The nitrogen adsorption of the outlet of the adsorption tower of the device is controlled at 78% (V) (in actual operation, it can also be adjusted between 30 and 78V%), and the second stage of the pressure swing adsorption gas separation device functions as the first stage pressure swing adsorption gas separation device.
  • the nitrogen in the outlet gas is further purified, so that the oxygen concentration at the outlet of the adsorption tower of the second stage of the pressure swing adsorption gas separation device is greater than 93% (V), up to 95W. To meet the needs of the next step.
  • Six adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption three-time pressure equalization program is run.
  • the four adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption one-time pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, reverse BD, vacuum VC, two-stage gas boost 2ER, two ends are 2E3R', two ends are 2E2R', both ends are raised 2E1R', most
  • the final step-up FR pressure swing adsorption process step the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption A, one equal drop E1D, reverse buck BD, one equal E1 R, and finally boost FR in one cycle.
  • the gas in the reverse step-down BD step enters the adsorption tower of the first stage pressure swing adsorption device to pressurize the adsorption tower that has completed the vacuum VC, and the second stage pressure swing adsorption device is in the adsorption step of the adsorption step.
  • the product gas discharged from the outlet is mainly oxygen and a small amount of argon.
  • the results of this example are that the oxygen concentration is greater than 93% (V), the nitrogen concentration is greater than 99% (V), and the oxygen recovery is greater than 96% (V).
  • Embodiment 35 of the present invention is a diagrammatic representation of Embodiment 35 of the present invention.
  • the raw material gas in this case is air.
  • the first stage of the pressure swing adsorption gas separation device, the bottom-up loading adsorbent in the adsorption tower is activated alumina and molecular sieve in turn; the second stage pressure swing adsorption gas separation device, in the adsorption tower
  • the loaded adsorbent is a molecular sieve.
  • This embodiment is a pressure swing adsorption oxygen generator. In the air, oxygen and argon are components of the difficult phase to be adsorbed, and nitrogen and water (steam) are components of the easily adsorbable phase.
  • the first stage of the pressure swing adsorption gas separation in this embodiment The nitrogen outlet of the adsorption tower of the device is controlled to be above 78% (V).
  • the second stage of the pressure swing adsorption gas separation device is to further purify the nitrogen in the outlet gas of the first stage of the pressure swing adsorption gas separation device to make the second stage pressure swing adsorption.
  • the oxygen concentration of the upper end of the adsorption tower of the gas separation device is greater than 93% (V), up to 95V%, to meet the needs of the next step.
  • Seven adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption four-time pressure equalization program is run.
  • the five adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption two-time pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • the step-up FR pressure swing adsorption process step the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption in one cycle, and the average adsorption E1 D, the second average E2D, the reverse buck BD, and the second average E2R , an E1 R, a final boost FR pressure swing adsorption process step, the reverse buck BD step gas enters the first stage of the pressure swing adsorption device adsorption tower to boost the adsorption tower that has completed the vacuum VC, the second stage
  • the product gas discharged from the outlet of the adsorption tower which is at the adsorption step of the pressure swing adsorption device is mainly oxygen and a small amount of argon gas
  • Embodiment 36 of the present invention is that the oxygen concentration is greater than 93% (V), and the nitrogen concentration is greater than 99.7% (V), oxygen.
  • the recovery is greater than 99% (V).
  • the raw material gas in this case is air.
  • the adsorbent in the adsorption tower of the first stage of the pressure swing adsorption gas separation device is activated alumina and molecular sieve in order from the bottom to the top; the adsorbent packed in the adsorption tower of the second stage pressure swing adsorption gas separation device is a molecular sieve.
  • This embodiment is a pressure swing adsorption oxygen generator. In the air, oxygen and argon are components of the difficult phase to be adsorbed, and nitrogen and water (steam) are components of the easily adsorbable phase.
  • the first stage of the pressure swing adsorption gas separation in this embodiment The nitrogen adsorption of the outlet of the adsorption tower of the device is controlled at 78% (V) (in actual operation, it can also be adjusted between 20 and 78 W), and the second stage of the pressure swing adsorption gas separation device functions as the first stage pressure swing adsorption gas separation device.
  • the nitrogen in the outlet gas is further purified, so that the oxygen concentration at the outlet of the adsorption tower of the second stage of the pressure swing adsorption gas separation device is greater than 93% (V), up to 95V%, to meet the needs of the next step.
  • Seven adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption four-time pressure equalization program is run.
  • the seven adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption two-time pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • step-up FR pressure swing adsorption process step the adsorption tower of the second stage pressure swing adsorption device sequentially undergoes adsorption in one cycle, and the average adsorption E1 D, the second average drop E2D, the downstream PP1, the downstream PP2 Smooth PP3, reverse BD, cleaning Pl, cleaning P2, cleaning P3, two equalizing E2R, one equalizing E1R, final boosting FR pressure swing adsorption process steps, and the mixture gas discharged by the PP1 step is directly passed through the flow regulation.
  • the adsorption tower of the vacuum VC is boosted, and the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly oxygen and a small amount of argon gas.
  • Example 37 of the present invention is that the oxygen concentration is greater than 93% (V), the nitrogen concentration is greater than 99.7% (V), and the oxygen recovery is greater than 99% (V).
  • Example 37 of the present invention is that the oxygen concentration is greater than 93% (V), the nitrogen concentration is greater than 99.7% (V), and the oxygen recovery is greater than 99% (V).
  • the raw material gas in this case is air.
  • the adsorbent in the adsorption tower of the first stage of the pressure swing adsorption gas separation device is activated alumina and molecular sieve in order from the bottom to the top; the adsorbent packed in the adsorption tower of the second stage pressure swing adsorption gas separation device is a molecular sieve.
  • This embodiment is a pressure swing adsorption oxygen generator. In the air, oxygen and argon are components of the difficult phase to be adsorbed, and nitrogen and water (steam) are components of the easily adsorbable phase.
  • the first stage of the pressure swing adsorption gas separation in this embodiment The nitrogen adsorption at the outlet of the adsorption tower of the device is controlled at 78% (V) (in actual operation, it can also be adjusted between 20 and 78V%), and the second-stage pressure swing adsorption gas separation device functions as the first pressure swing adsorption gas separation device.
  • the nitrogen in the outlet gas is further purified, so that the oxygen concentration at the outlet of the adsorption tower of the second stage of the pressure swing adsorption gas separation device is greater than 93% (V), up to 95V%, to meet the needs of the next step.
  • Seven adsorption towers constitute the first stage pressure swing adsorption device, and the single tower adsorption four-time pressure equalization program is run.
  • the seven adsorption towers constitute the second stage pressure swing adsorption device, and the single tower adsorption two-time pressure equalization program is operated.
  • the adsorption tower of the first stage pressure swing adsorption device successively undergoes adsorption A in one cycle, 2E1D' at both ends, 2E2D' at both ends, 2E3D' at both ends, and 2E4D at both ends.
  • the adsorption tower of the second stage pressure swing adsorption device successively undergoes adsorption A, one equal E1D, two equal E2D, a smooth PP1, a PP2, a PP3, and a reverse phase in one cycle.
  • the mixture of the mixture discharged by the PP step 1 is directly cleaned by flow adjustment, and the cleaning has been completed.
  • the adsorbed impurities on the adsorbent are desorbed, and the mixture gas discharged in the step of discharging the PP2 is directly cleaned by the flow rate to clean the adsorption tower which has been cleaned in the P1 step, and the mixed gas passing through the PP3 step passes through the flow.
  • the adsorption tower that has completed the reverse BD step desorbs the adsorbed impurities on the adsorbent, and the reverse pressure reduction BD step and the cleaning P step gas enter the first stage pressure swing adsorption device adsorption tower to complete the vacuum pumping VC
  • the adsorption tower is boosted, and the product gas discharged from the outlet of the adsorption tower which is in the adsorption step of the second stage pressure swing adsorption device is mainly oxygen and a small amount of argon gas.
  • the result of this example is that the oxygen concentration is greater than 93% (V), the nitrogen concentration is greater than 99.7% (V), and the oxygen recovery is greater than 99% (V) o.
  • the present invention is not limited to the above-mentioned range application, and can be applied to all of the easily adsorbable phase products obtained from the mixed gas or the difficult-adsorbed phase products obtained from the mixed gas, and also applied to all of the easily adsorbable gases from the mixed gas.
  • the easily adsorbable phase and the poorly adsorbed phase of the present invention may be one component or may be one or more components.
  • the invention is applicable to industrial fields such as chemical industry, petrochemical, pharmaceutical, building materials and environmental protection.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Separation Of Gases By Adsorption (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

La présente invention concerne un processus d'adsorption par variation de la pression de recyclage complet à deux étages en vue de séparer des gaz, qui consiste à séparer plus d'éléments adsorbables et moins d'éléments adsorbable d'un mélange de gaz pour obtenir un produit qui est un élément plus adsorbable ou moins adsorbable ou les deux. On fait fonctionner en série un adsorbeur par variation de pression à deux étages. Le mélange de gaz est alimenté dans le système de séparation de gaz par adsorption par variation de pression de premier étage et l'élément le plus adsorbable de ce mélange de gaz est adsorbé puis il est extrait en produit. Le mélange de gaz semi-fini en provenance de la sortie de la tour d'adsorption par variation de pression de première étage est alimenté dans le système de séparation de gaz d'absorption par variation de pression de second étage. L'élément le plus adsorbable du mélange de gaz semi-fini est adsorbé à nouveau et, l'élément le moins adsorbable est alimenté dans l'étage suivant. Le gaz du système de séparation de gaz par adsorption par variation de pression de second étage, à part pour l'élément le moins adsorbable alimenté dans l'étage suivant, est réintroduit dans le système de séparation de gaz par adsorption par variation de pression de premier étage de façon à augmenter la pression. La tour d'adsorption par variation pression de premier étage dans une période cyclique comprend les étapes successives suivantes : étape d'adsorption A, égalisation de pression aux deux extrémités et réduction 2ED', réduction par pression inverse BD, suralimentation 2ER par pression de gaz de second étage, égalisation par pression aux deux extrémité et suralimentation 2ER'et suralimentation finale FR. La tour d'adsorption par variation pression de second étage dans une période cyclique comprend les étapes successives suivantes : étape d'adsorption A, la séquence d'égalisation par pression et réduction ED, réduction par pression inverse BD, égalisation par pression inverse et suralimentation ER et suralimentation finale FR.
PCT/CN2005/000641 2004-06-11 2005-05-09 Processus d'adsorption par variation de la pression de recyclage complet a deux etages en vue de separer des gaz WO2005120681A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US11/570,312 US8545601B2 (en) 2004-06-11 2005-05-09 Two-stage complete recycle pressure-swing adsorption process for gas separation
DE602005026125T DE602005026125D1 (de) 2004-06-11 2005-05-09 Lständiger rezyklierung für die gastrennung
EA200700011A EA012820B1 (ru) 2004-06-11 2005-05-09 Способ разделения газов
EP05745102A EP1772182B1 (fr) 2004-06-11 2005-05-09 Processus d'adsorption par variation de la pression de recyclage complet a deux etages en vue de separer des gaz
AT05745102T ATE496676T1 (de) 2004-06-11 2005-05-09 Zweistufiges druckwechseladsorptionssystem mit vollständiger rezyklierung für die gastrennung
PL05745102T PL1772182T3 (pl) 2004-06-11 2005-05-09 Oparty na adsorpcji pod zmiennym ciśnieniem dwuetapowy sposób rozdzielania gazu z pełnym zawracaniem
AU2005251848A AU2005251848B2 (en) 2004-06-11 2005-05-09 A two-stage complete recycle pressure-swing adsorption process for gas seperation
JP2007526170A JP4579983B2 (ja) 2004-06-11 2005-05-09 二段全回収変圧吸着によるガス分離方法

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN200410046598.4 2004-06-11
CNB2004100465984A CN1250321C (zh) 2004-06-11 2004-06-11 一种两段全回收变压吸附气体分离方法

Publications (1)

Publication Number Publication Date
WO2005120681A1 true WO2005120681A1 (fr) 2005-12-22

Family

ID=34602013

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2005/000641 WO2005120681A1 (fr) 2004-06-11 2005-05-09 Processus d'adsorption par variation de la pression de recyclage complet a deux etages en vue de separer des gaz

Country Status (11)

Country Link
US (1) US8545601B2 (fr)
EP (1) EP1772182B1 (fr)
JP (1) JP4579983B2 (fr)
CN (1) CN1250321C (fr)
AT (1) ATE496676T1 (fr)
AU (1) AU2005251848B2 (fr)
DE (1) DE602005026125D1 (fr)
EA (1) EA012820B1 (fr)
ES (1) ES2360346T3 (fr)
PL (1) PL1772182T3 (fr)
WO (1) WO2005120681A1 (fr)

Families Citing this family (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1287886C (zh) * 2004-06-11 2006-12-06 成都天立化工科技有限公司 一种改进的两段变压吸附制富氧方法
CA2667467C (fr) * 2006-10-27 2015-03-24 Questair Technologies Inc. Reformeur a variation de pression compact
CN102080000B (zh) * 2010-12-13 2013-05-22 甘肃银光聚银化工有限公司 一种利用变压吸附法从水煤气中分离并提纯co的方法
CN102078740B (zh) * 2010-12-13 2013-02-27 甘肃银光聚银化工有限公司 一种利用变压吸附法从水煤气中分离并提纯氢气的方法
US8496733B2 (en) * 2011-01-11 2013-07-30 Praxair Technology, Inc. Large scale pressure swing adsorption systems having process cycles operating in normal and turndown modes
JP5968252B2 (ja) 2013-03-04 2016-08-10 大阪瓦斯株式会社 メタンガス濃縮方法
CN103223288B (zh) * 2013-04-08 2015-01-21 河南心连心化肥有限公司 变压吸附脱碳装置及工艺
EP2823872A3 (fr) 2014-09-11 2015-05-06 Air Products And Chemicals, Inc. Procédé d'adsorption à pression alternée
US9381460B2 (en) 2014-09-11 2016-07-05 Air Products And Chemicals, Inc. Pressure swing adsorption process
CN105097633A (zh) 2015-06-24 2015-11-25 合肥京东方光电科技有限公司 一种用于离线真空吸附基板的承载机构和基板传送方法
BR112018070204B1 (pt) * 2016-03-31 2023-01-31 Inventys Thermal Technologies Inc Processo de separação de gás adsortivo que emprega vapor para regeneração
CN106943842A (zh) * 2017-04-19 2017-07-14 成都赛普瑞兴科技有限公司 一种变压吸附气体分离方法
US10632414B2 (en) * 2018-01-25 2020-04-28 Uop Llc Integration of pressure swing adsorption and hydroprocessing for improved hydrogen utilization
CN108329962B (zh) * 2018-03-01 2021-05-14 中国石油化工股份有限公司 天然气中氮气脱除的方法和装置
CN110574572A (zh) * 2019-10-18 2019-12-17 福建省莆田市三月三农业科技有限公司 一种增氧系统及带有增氧系统的植物工厂
EP4337810A1 (fr) * 2021-05-14 2024-03-20 Amogy Inc. Systèmes et procédés de traitement d'ammoniac
US11724245B2 (en) 2021-08-13 2023-08-15 Amogy Inc. Integrated heat exchanger reactors for renewable fuel delivery systems
US11994061B2 (en) 2021-05-14 2024-05-28 Amogy Inc. Methods for reforming ammonia
JP2024521417A (ja) 2021-06-11 2024-05-31 アモジー インコーポレイテッド アンモニアを処理するためのシステムおよび方法
US11539063B1 (en) 2021-08-17 2022-12-27 Amogy Inc. Systems and methods for processing hydrogen
CN114748971B (zh) * 2022-03-16 2023-03-03 四川天采科技有限责任公司 一种旋转分配器用于合成气提纯h2与co的方法
CN115354307B (zh) * 2022-09-23 2023-08-18 拓荆科技股份有限公司 一种真空加热衬底设备
US11834334B1 (en) 2022-10-06 2023-12-05 Amogy Inc. Systems and methods of processing ammonia
US11866328B1 (en) 2022-10-21 2024-01-09 Amogy Inc. Systems and methods for processing ammonia
US11795055B1 (en) 2022-10-21 2023-10-24 Amogy Inc. Systems and methods for processing ammonia

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2183832A1 (fr) * 1995-08-21 1997-02-22 Glenn C. Stoner Procede ameliore de recuperation de l'helium
CN1215627A (zh) * 1997-10-24 1999-05-05 化学工业部西南化工研究设计院 从含一氧化碳混合气中提纯一氧化碳的变压吸附法
US5993517A (en) * 1998-03-17 1999-11-30 The Boc Group, Inc. Two stage pressure swing adsorption process
US6102985A (en) * 1998-11-25 2000-08-15 Air Products And Chemicals, Inc. Pressure swing adsorption process and system with dual product storage tanks
CN1347747A (zh) * 2001-07-31 2002-05-08 成都天立化工科技有限公司 尿素生产中氢氮气高回收率两段变压吸附脱碳工艺方法

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3046267A1 (de) * 1980-12-09 1982-07-15 Linde Ag, 6200 Wiesbaden Adsorptionsverfahren
DE3205505A1 (de) * 1982-02-16 1983-08-25 Linde Ag, 6200 Wiesbaden Verfahren zum betrieb einer zyklisch arbeitenden druckwechsel-adsorptionsanlage
JPS59207803A (ja) * 1983-02-10 1984-11-26 Nippon Kagaku Gijutsu Kk 二段圧力スイング吸着法による水素精製方法
JPS607920A (ja) * 1983-06-29 1985-01-16 Hitachi Ltd 非凝縮性混合ガスの分離方法
DE3543468A1 (de) * 1985-12-09 1987-06-11 Linde Ag Druckwechseladsorptionsverfahren
EP0380723B1 (fr) * 1989-02-01 1994-04-06 Kuraray Chemical Co., Ltd. Procédé pour séparer des gaz contenant de l'azote avec un système d'adsorption à pression alternée
KR970008347B1 (ko) * 1994-04-12 1997-05-23 한국에너지기술연구소 암모니아 퍼지가스에서 아르곤 및 수소를 고농도로 분리하는 흡착분리방법과 그 장치
US5520720A (en) * 1994-11-30 1996-05-28 The Boc Group, Inc. Pressure swing adsorption process
US5914455A (en) * 1997-09-30 1999-06-22 The Boc Group, Inc. Air purification process

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2183832A1 (fr) * 1995-08-21 1997-02-22 Glenn C. Stoner Procede ameliore de recuperation de l'helium
CN1215627A (zh) * 1997-10-24 1999-05-05 化学工业部西南化工研究设计院 从含一氧化碳混合气中提纯一氧化碳的变压吸附法
US5993517A (en) * 1998-03-17 1999-11-30 The Boc Group, Inc. Two stage pressure swing adsorption process
US6102985A (en) * 1998-11-25 2000-08-15 Air Products And Chemicals, Inc. Pressure swing adsorption process and system with dual product storage tanks
CN1347747A (zh) * 2001-07-31 2002-05-08 成都天立化工科技有限公司 尿素生产中氢氮气高回收率两段变压吸附脱碳工艺方法

Also Published As

Publication number Publication date
EP1772182B1 (fr) 2011-01-26
ATE496676T1 (de) 2011-02-15
EA200700011A1 (ru) 2007-08-31
EP1772182A4 (fr) 2008-12-31
US8545601B2 (en) 2013-10-01
US20070221060A1 (en) 2007-09-27
ES2360346T3 (es) 2011-06-03
AU2005251848B2 (en) 2008-09-11
EP1772182A1 (fr) 2007-04-11
PL1772182T3 (pl) 2011-06-30
JP2008501514A (ja) 2008-01-24
AU2005251848A1 (en) 2005-12-22
CN1250321C (zh) 2006-04-12
JP4579983B2 (ja) 2010-11-10
DE602005026125D1 (de) 2011-03-10
EA012820B1 (ru) 2009-12-30
CN1583221A (zh) 2005-02-23

Similar Documents

Publication Publication Date Title
WO2005120681A1 (fr) Processus d'adsorption par variation de la pression de recyclage complet a deux etages en vue de separer des gaz
KR100300939B1 (ko) 진공 압력 순환 흡착 방법
CA2189232C (fr) Procede de recuperation de gaz riche en oxygene
CA2160046C (fr) Procede d'adsorption modulee en pression
JP3232003B2 (ja) 圧力スイング式吸着法における還流
WO2005120680A1 (fr) Processus d'adsorption modulee en pression a deux etages ameliore de production d'oxygene enrichi
US4475929A (en) Selective adsorption process
US4375363A (en) Selective adsorption process for production of ammonia synthesis gas mixtures
WO2018108066A1 (fr) Procédé de séparation et de recyclage de gaz sec de raffinerie
JP5184885B2 (ja) 三段変圧吸着装置による酸素の生産方法
CN101249370B (zh) 循环有价值气体的变压吸附方法
KR20080066973A (ko) 산소 생산을 위한 압력 스윙 흡착 방법
US6048384A (en) PSA process and system using simultaneous top and bottom evacuation of absorbent bed
CN103585856A (zh) 一种多回流的变压吸附方法
KR20050100690A (ko) 오프 가스 공급 방법, 및 목적 가스 정제 시스템
WO2022068165A1 (fr) Procédé efficace de production d'oxygène vpsa et son système
US20140069275A1 (en) Low energy cyclic psa process
CN100490939C (zh) 采用变压吸附技术从变换气中脱除二氧化碳的方法
JPH11239709A (ja) 可変製造速度で吸着により気体分離する方法
WO2023064977A1 (fr) Procédé et installation d'adsorption modulée en pression sous vide pour la production de dioxyde de carbone pur à partir de gaz de dégagement industriel contenant du co 2
CN108821248A (zh) 一种新型节能高效型psa制氮设备
CN116390797A (zh) 用于从低品级氢气生产超高纯氢气的工艺和设备
JPH10225609A (ja) パラメトリックガスクロマトグラフィーによる気体のバルク分離方法
JP7388731B2 (ja) 圧力スイング吸着装置、および、ガス生成方法
CN100434139C (zh) 一种改进的一段变压吸附气体分离方法

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KM KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NG NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SM SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GM KE LS MW MZ NA SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IS IT LT LU MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
WWE Wipo information: entry into national phase

Ref document number: 2007526170

Country of ref document: JP

NENP Non-entry into the national phase

Ref country code: DE

WWW Wipo information: withdrawn in national office

Ref document number: DE

WWE Wipo information: entry into national phase

Ref document number: 2005745102

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 3814/KOLNP/2006

Country of ref document: IN

WWE Wipo information: entry into national phase

Ref document number: 2005251848

Country of ref document: AU

WWE Wipo information: entry into national phase

Ref document number: 200700011

Country of ref document: EA

ENP Entry into the national phase

Ref document number: 2005251848

Country of ref document: AU

Date of ref document: 20050509

Kind code of ref document: A

WWP Wipo information: published in national office

Ref document number: 2005251848

Country of ref document: AU

WWP Wipo information: published in national office

Ref document number: 2005745102

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2007221060

Country of ref document: US

Ref document number: 11570312

Country of ref document: US

WWP Wipo information: published in national office

Ref document number: 11570312

Country of ref document: US